CN104671572A - 一种火电厂脱硫废水电渗析软化浓缩处理系统及方法 - Google Patents
一种火电厂脱硫废水电渗析软化浓缩处理系统及方法 Download PDFInfo
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- CN104671572A CN104671572A CN201510030770.5A CN201510030770A CN104671572A CN 104671572 A CN104671572 A CN 104671572A CN 201510030770 A CN201510030770 A CN 201510030770A CN 104671572 A CN104671572 A CN 104671572A
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- 239000002351 wastewater Substances 0.000 title claims abstract description 71
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 54
- 230000003009 desulfurizing Effects 0.000 title claims abstract description 53
- 238000000909 electrodialysis Methods 0.000 title claims abstract description 29
- 238000006243 chemical reaction Methods 0.000 claims abstract description 49
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances data:image/svg+xml;base64,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 data:image/svg+xml;base64,PD94bWwgdmVyc2lvbj0nMS4wJyBlbmNvZGluZz0naXNvLTg4NTktMSc/Pgo8c3ZnIHZlcnNpb249JzEuMScgYmFzZVByb2ZpbGU9J2Z1bGwnCiAgICAgICAgICAgICAgeG1sbnM9J2h0dHA6Ly93d3cudzMub3JnLzIwMDAvc3ZnJwogICAgICAgICAgICAgICAgICAgICAgeG1sbnM6cmRraXQ9J2h0dHA6Ly93d3cucmRraXQub3JnL3htbCcKICAgICAgICAgICAgICAgICAgICAgIHhtbG5zOnhsaW5rPSdodHRwOi8vd3d3LnczLm9yZy8xOTk5L3hsaW5rJwogICAgICAgICAgICAgICAgICB4bWw6c3BhY2U9J3ByZXNlcnZlJwp3aWR0aD0nODVweCcgaGVpZ2h0PSc4NXB4JyB2aWV3Qm94PScwIDAgODUgODUnPgo8IS0tIEVORCBPRiBIRUFERVIgLS0+CjxyZWN0IHN0eWxlPSdvcGFjaXR5OjEuMDtmaWxsOiNGRkZGRkY7c3Ryb2tlOm5vbmUnIHdpZHRoPSc4NS4wJyBoZWlnaHQ9Jzg1LjAnIHg9JzAuMCcgeT0nMC4wJz4gPC9yZWN0Pgo8dGV4dCB4PScxMy4zJyB5PSc1My42JyBjbGFzcz0nYXRvbS0wJyBzdHlsZT0nZm9udC1zaXplOjIzcHg7Zm9udC1zdHlsZTpub3JtYWw7Zm9udC13ZWlnaHQ6bm9ybWFsO2ZpbGwtb3BhY2l0eToxO3N0cm9rZTpub25lO2ZvbnQtZmFtaWx5OnNhbnMtc2VyaWY7dGV4dC1hbmNob3I6c3RhcnQ7ZmlsbDojRTg0MjM1JyA+SDwvdGV4dD4KPHRleHQgeD0nMjguMicgeT0nNjIuOScgY2xhc3M9J2F0b20tMCcgc3R5bGU9J2ZvbnQtc2l6ZToxNXB4O2ZvbnQtc3R5bGU6bm9ybWFsO2ZvbnQtd2VpZ2h0Om5vcm1hbDtmaWxsLW9wYWNpdHk6MTtzdHJva2U6bm9uZTtmb250LWZhbWlseTpzYW5zLXNlcmlmO3RleHQtYW5jaG9yOnN0YXJ0O2ZpbGw6I0U4NDIzNScgPjI8L3RleHQ+Cjx0ZXh0IHg9JzM1LjAnIHk9JzUzLjYnIGNsYXNzPSdhdG9tLTAnIHN0eWxlPSdmb250LXNpemU6MjNweDtmb250LXN0eWxlOm5vcm1hbDtmb250LXdlaWdodDpub3JtYWw7ZmlsbC1vcGFjaXR5OjE7c3Ryb2tlOm5vbmU7Zm9udC1mYW1pbHk6c2Fucy1zZXJpZjt0ZXh0LWFuY2hvcjpzdGFydDtmaWxsOiNFODQyMzUnID5PPC90ZXh0Pgo8L3N2Zz4K O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 48
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,PD94bWwgdmVyc2lvbj0nMS4wJyBlbmNvZGluZz0naXNvLTg4NTktMSc/Pgo8c3ZnIHZlcnNpb249JzEuMScgYmFzZVByb2ZpbGU9J2Z1bGwnCiAgICAgICAgICAgICAgeG1sbnM9J2h0dHA6Ly93d3cudzMub3JnLzIwMDAvc3ZnJwogICAgICAgICAgICAgICAgICAgICAgeG1sbnM6cmRraXQ9J2h0dHA6Ly93d3cucmRraXQub3JnL3htbCcKICAgICAgICAgICAgICAgICAgICAgIHhtbG5zOnhsaW5rPSdodHRwOi8vd3d3LnczLm9yZy8xOTk5L3hsaW5rJwogICAgICAgICAgICAgICAgICB4bWw6c3BhY2U9J3ByZXNlcnZlJwp3aWR0aD0nODVweCcgaGVpZ2h0PSc4NXB4JyB2aWV3Qm94PScwIDAgODUgODUnPgo8IS0tIEVORCBPRiBIRUFERVIgLS0+CjxyZWN0IHN0eWxlPSdvcGFjaXR5OjEuMDtmaWxsOiNGRkZGRkY7c3Ryb2tlOm5vbmUnIHdpZHRoPSc4NS4wJyBoZWlnaHQ9Jzg1LjAnIHg9JzAuMCcgeT0nMC4wJz4gPC9yZWN0Pgo8dGV4dCB4PSczLjQnIHk9JzUyLjAnIGNsYXNzPSdhdG9tLTAnIHN0eWxlPSdmb250LXNpemU6MjBweDtmb250LXN0eWxlOm5vcm1hbDtmb250LXdlaWdodDpub3JtYWw7ZmlsbC1vcGFjaXR5OjE7c3Ryb2tlOm5vbmU7Zm9udC1mYW1pbHk6c2Fucy1zZXJpZjt0ZXh0LWFuY2hvcjpzdGFydDtmaWxsOiNFODQyMzUnID5IPC90ZXh0Pgo8dGV4dCB4PScxNi4yJyB5PSc1Mi4wJyBjbGFzcz0nYXRvbS0wJyBzdHlsZT0nZm9udC1zaXplOjIwcHg7Zm9udC1zdHlsZTpub3JtYWw7Zm9udC13ZWlnaHQ6bm9ybWFsO2ZpbGwtb3BhY2l0eToxO3N0cm9rZTpub25lO2ZvbnQtZmFtaWx5OnNhbnMtc2VyaWY7dGV4dC1hbmNob3I6c3RhcnQ7ZmlsbDojRTg0MjM1JyA+TzwvdGV4dD4KPHRleHQgeD0nMzAuMScgeT0nNDQuMCcgY2xhc3M9J2F0b20tMCcgc3R5bGU9J2ZvbnQtc2l6ZToxM3B4O2ZvbnQtc3R5bGU6bm9ybWFsO2ZvbnQtd2VpZ2h0Om5vcm1hbDtmaWxsLW9wYWNpdHk6MTtzdHJva2U6bm9uZTtmb250LWZhbWlseTpzYW5zLXNlcmlmO3RleHQtYW5jaG9yOnN0YXJ0O2ZpbGw6I0U4NDIzNScgPi08L3RleHQ+Cjx0ZXh0IHg9JzQ5LjcnIHk9JzUyLjAnIGNsYXNzPSdhdG9tLTEnIHN0eWxlPSdmb250LXNpemU6MjBweDtmb250LXN0eWxlOm5vcm1hbDtmb250LXdlaWdodDpub3JtYWw7ZmlsbC1vcGFjaXR5OjE7c3Ryb2tlOm5vbmU7Zm9udC1mYW1pbHk6c2Fucy1zZXJpZjt0ZXh0LWFuY2hvcjpzdGFydDtmaWxsOiMzQjQxNDMnID5OPC90ZXh0Pgo8dGV4dCB4PSc2My41JyB5PSc1Mi4wJyBjbGFzcz0nYXRvbS0xJyBzdHlsZT0nZm9udC1zaXplOjIwcHg7Zm9udC1zdHlsZTpub3JtYWw7Zm9udC13ZWlnaHQ6bm9ybWFsO2ZpbGwtb3BhY2l0eToxO3N0cm9rZTpub25lO2ZvbnQtZmFtaWx5OnNhbnMtc2VyaWY7dGV4dC1hbmNob3I6c3RhcnQ7ZmlsbDojM0I0MTQzJyA+YTwvdGV4dD4KPHRleHQgeD0nNzQuMicgeT0nNDQuMCcgY2xhc3M9J2F0b20tMScgc3R5bGU9J2ZvbnQtc2l6ZToxM3B4O2ZvbnQtc3R5bGU6bm9ybWFsO2ZvbnQtd2VpZ2h0Om5vcm1hbDtmaWxsLW9wYWNpdHk6MTtzdHJva2U6bm9uZTtmb250LWZhbWlseTpzYW5zLXNlcmlmO3RleHQtYW5jaG9yOnN0YXJ0O2ZpbGw6IzNCNDE0MycgPis8L3RleHQ+Cjwvc3ZnPgo= [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 45
- 239000000701 coagulant Substances 0.000 claims abstract description 34
- 230000001112 coagulant Effects 0.000 claims abstract description 22
- 238000002425 crystallisation Methods 0.000 claims abstract description 21
- 230000005712 crystallization Effects 0.000 claims abstract description 21
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Chemical compound 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Abstract
本发明公开了一种火电厂脱硫废水电渗析软化浓缩处理系统及方法，包括原水池、第一反应池、第二反应池、第一澄清器、第二澄清器、中间水池、电渗析装置、淡水池、浓水池、纯碱储罐、氢氧化钠储罐、混凝剂储罐、助凝剂储罐、加药装置及蒸发结晶系统。本发明可以实现对脱硫废水的处理，并且操作简单，成本低。
Description
技术领域
[0001] 本发明涉及一种浓缩处理系统及方法，具体涉及一种火电厂脱硫废水电渗析软化浓缩处理系统及方法。
背景技术
[0002] 目前，国内外火电厂常见的脱硫废水处理工艺主要为:水力除灰、单独设置化学处理系统(主要为三联箱处理)、蒸发等方法。其中蒸发处理是通过蒸发及结晶装置使脱硫废水分离成高品质的水蒸气和固体废物，以便于实现全厂废水零排放。采用蒸发结晶方法处理脱硫废水存在的缺点是:投资很高，因全部脱硫废水都进行蒸发，运行费用很高。因此，需要对脱硫废水进行减量处理，降低蒸发结晶系统的处理成本。
[0003] 用于脱硫废水减量处理的工艺主要包括反渗透以及纳滤等。由于脱硫废水含盐量偏高，且富含有机物和结垢性物质，采用反渗透进行浓缩减量，预处理工艺要求严格，而且系统回收率控制的偏低，一般在50%左右。采用纳滤进行脱硫废水减量处理，纳滤对一价离子的去除率偏大，产水无法直接回用，需要对纳滤产水进一步脱盐才能达到回用要求，工艺流程偏长，处理成本较高。因此，需要探索合适的脱硫废水减量处理工艺。
发明内容
[0004] 本发明的目的在于克服上述现有技术的缺点，提供了一种火电厂脱硫废水电渗析软化浓缩处理系统及方法，该系统及方法可以实现对脱硫废水的处理，并且操作简单，成本低。
[0005] 为达到上述目的，本发明所述的火电厂脱硫废水电渗析软化浓缩处理系统包括原水池、第一反应池、第二反应池、第一澄清器、第二澄清器、中间水池、电渗析装置、淡水池、浓水池、纯碱储罐、氢氧化钠储罐、混凝剂储罐、助凝剂储罐、加药装置及蒸发结晶系统；
[0006] 所述第一反应池的入口与原水池的出口及氢氧化钠储罐的出口相连通，第一反应池的出口与混凝剂储罐的出口及助凝剂储罐的出口通过管道并管后与第一澄清器的入口相连通，第一澄清器顶部的出口及纯碱储罐的出口与第二反应池的入口相连通，第二反应池的出口与第二澄清器的入口相连通，第二澄清器顶部的出口与中间水池的入口相连通，中间水池的出口与加药装置的出口通过管道并管后与电渗析装置的入口相连通，电渗析装置的浓水出口与浓水池的入口相连通，电渗析装置的淡水出口与淡水池的入口相连通，浓水池的出口与蒸发结晶系统的入口相连通。
[0007] 还包括去压滤机，去压滤机的入口与第一澄清器底部的污泥出口及第二澄清器底部的污泥出口相连通。
[0008] 所述加药装置内装有盐酸。
[0009] 本发明所述的火电厂脱硫废水电渗析软化浓缩处理方法包括以下步骤:
[0010] I)火电厂产生的脱硫废水进入原水池中，原水池中的脱硫废水进入到第一反应池中，同时氢氧化钠储罐中的氢氧化钠进入第一反应池中，使第一反应池中脱硫废水的pH值调整至10-11 ;经第一反应池处理后的脱硫废水与混凝剂储罐输出的混凝剂及助凝剂储罐中的助凝剂混合后输入到第一澄清器中，并在第一澄清器混凝沉淀，进而去除脱硫废水中Mg2+以及部分重金属离子；
[0011 ] 2)经第一澄清器处理后的脱硫废水进入到第二反应池中，并与纯碱储罐输出的纯碱在第二反应池中进行反应，使脱硫废水中的Ca2+生成CaCO3，并去除剩余的重金属离子，同时经第二反应池处理后的脱硫废水进入到第二澄清器中，并在第二澄清器中进行沉淀，经在第二澄清器中沉淀的脱硫废水进入到中间水池中；
[0012] 3)中间水池中的脱硫废水与加药装置中输出的盐酸进行混合后，使脱硫废水的pH值调整至9-10，然后进入到电渗析装置，并经电渗析装置分离为淡水及浓缩水，其中淡水进入到淡水池中回收利用，浓缩水经蒸发结晶系统蒸发结晶并回收。
[0013] 进入到第二反应池中的脱硫废水中Ca2+的摩尔质量与进入到第二反应池中纯碱的摩尔质量的比例为1:1。
[0014] 本发明具有以下有益效果:
[0015] 本发明所述的火电厂脱硫废水电渗析软化浓缩处理系统及方法在对火电厂脱硫废水进行处理时，先将通过氢氧化钠调节脱硫废水的pH值，再通过混凝剂储罐内的混凝剂及助凝剂储罐中的助凝剂进行混凝沉淀，使Mg2+以及部分重金属离子进行沉积，再加入纯碱储罐输出的纯碱，使脱硫废水中的Ca2+及剩余重金属离子进行沉淀，然后调节pH值，并通过电渗析装置进行电渗析后分离为淡水及浓缩水，浓缩水经蒸发结晶系统蒸发结晶后回收，淡水直接进行回收，从而实现对脱硫废水的处理，同时可有效降低蒸发结晶装置处理的废水量，还能回收利用工业盐，大大降低了能源消耗，可有效解决脱硫废水循环利用问题，可实现火电厂废水“零排放”。而且工艺设计简单，系统运行稳定，可实现全自动运行，操作运行简单方便，成本低。
[0016] 进一步，本发明还包括去压滤机，去压滤机的入口与第一澄清器底部的污泥出口及第二澄清器底部的污泥出口相连通，第一澄清器与第二澄清器底部的污泥经去压滤机进行回收，节能环保。
附图说明
[0017] 图1为本发明的结构示意图。
[0018] 其中，I为原水池、2为第一反应池、3为氢氧化钠储罐、4为第一澄清器、5为混凝剂储罐、6为助凝剂储罐、7为第二反应池、8为纯碱储罐、9为第二澄清器、10为中间水池、11为电渗析装置、12为加药装置、13为浓水池、14为淡水池、15为去压滤机、16为蒸发结晶系统。
具体实施方式
[0019] 下面结合附图对本发明做进一步详细描述:
[0020] 参考图1，本发明所述的火电厂脱硫废水电渗析软化浓缩处理系统包括原水池1、第一反应池2、第二反应池7、第一澄清器4、第二澄清器9、中间水池10、电渗析装置11、淡水池14、浓水池13、纯碱储罐8、氢氧化钠储罐3、混凝剂储罐5、助凝剂储罐6、加药装置12及蒸发结晶系统16 ;
[0021] 所述第一反应池2的入口与原水池I的出口及氢氧化钠储罐3的出口相连通，第一反应池2的出口与混凝剂储罐5的出口及助凝剂储罐6的出口通过管道并管后与第一澄清器4的入口相连通，第一澄清器4顶部的出口及纯碱储罐8的出口与第二反应池7的入口相连通，第二反应池7的出口与第二澄清器9的入口相连通，第二澄清器9顶部的出口与中间水池10的入口相连通，中间水池10的出口与加药装置12的出口通过管道并管后与电渗析装置11的入口相连通，电渗析装置11的浓水出口与浓水池13的入口相连通，电渗析装置11的淡水出口与淡水池14的入口相连通，浓水池13的出口与蒸发结晶系统16的入口相连通。
[0022] 本发明还包括去压滤机15，去压滤机15的入口与第一澄清器4底部的污泥出口及第二澄清器9底部的污泥出口相连通；加药装置12内装有盐酸。
[0023] 本发明所述的火电厂脱硫废水电渗析软化浓缩处理方法包括以下步骤:
[0024] I)火电厂产生的脱硫废水进入原水池I中，原水池I中的脱硫废水进入到第一反应池2中，同时氢氧化钠储罐3中的氢氧化钠进入第一反应池2中，使第一反应池2中脱硫废水的PH值调整至10-11 ;经第一反应池2处理后的脱硫废水与混凝剂储罐5输出的混凝剂及助凝剂储罐6中的助凝剂混合后输入到第一澄清器4中，并在第一澄清器4混凝沉淀，进而去除脱硫废水中Mg2+以及部分重金属离子；
[0025] 2)经第一澄清器4处理后的脱硫废水进入到第二反应池7中，并与纯碱储罐8输出的纯碱在第二反应池7中进行反应，使脱硫废水中的Ca2+生成CaCO 3，并去除剩余的重金属离子，同时经第二反应池7处理后的脱硫废水进入到第二澄清器9中，并在第二澄清器9中进行沉淀，经在第二澄清器9中沉淀的脱硫废水进入到中间水池10中；需要说明的是，进入到中间水池10中的水中的有机物占原始脱硫废水中有机物的30-40%，保证后续系统的稳定运行。
[0026] 3)中间水池10中的脱硫废水与加药装置12中输出的药进行混合后，使脱硫废水的pH值调整至9-10，然后进入到电渗析装置11，并经电渗析装置11分离为淡水及浓缩水，其中淡水进入到淡水池14中回收利用，浓缩水经蒸发结晶系统16蒸发结晶并回收。
[0027] 进入到第二反应池7中的脱硫废水中Ca2+的摩尔质量与进入到第二反应池7中纯碱的摩尔质量的比例为1:1。
[0028] 电渗析装置11的电源电压控制根据电渗析装置11的级数和段数确定，脱盐率控制在70%，回收率控制在60%〜80%，操作温度控制在20°C〜30°C。电渗析出水分为淡水和浓水，淡水进入淡水池14，可直接回用，浓水主要含氯化钠、大分子物质，进入浓水池13，进行蒸发结晶。另外，通过调整混凝剂及助凝剂的量，第一澄清器4输出的水中Mg2+浓度< 20mg/L ;通过控制纯碱的添加量，是第二澄清器9输出的水中Ca2+浓度< 20mg/L。
Claims (5)
1.一种火电厂脱硫废水电渗析软化浓缩处理系统，其特征在于，包括原水池(I)、第一反应池(2)、第二反应池(7)、第一澄清器(4)、第二澄清器(9)、中间水池(10)、电渗析装置(11)、淡水池(14)、浓水池(13)、纯碱储罐(8)、氢氧化钠储罐(3)、混凝剂储罐(5)、助凝剂储罐(6)、加药装置(12)及蒸发结晶系统(16); 所述第一反应池(2)的入口与原水池(I)的出口及氢氧化钠储罐(3)的出口相连通，第一反应池(2)的出口与混凝剂储罐(5)的出口及助凝剂储罐(6)的出口通过管道并管后与第一澄清器⑷的入口相连通，第一澄清器⑷顶部的出口及纯碱储罐⑶的出口与第二反应池(7)的入口相连通，第二反应池(7)的出口与第二澄清器(9)的入口相连通，第二澄清器(9)顶部的出口与中间水池(10)的入口相连通，中间水池(10)的出口与加药装置(12)的出口通过管道并管后与电渗析装置(11)的入口相连通，电渗析装置(11)的浓水出口与浓水池(13)的入口相连通，电渗析装置(11)的淡水出口与淡水池(14)的入口相连通，浓水池(13)的出口与蒸发结晶系统(16)的入口相连通。
2.根据权利要求1所述的火电厂脱硫废水电渗析软化浓缩处理系统，其特征在于，还包括去压滤机(15)，去压滤机(15)的入口与第一澄清器(4)底部的污泥出口及第二澄清器(9)底部的污泥出口相连通。
3.根据权利要求1所述的火电厂脱硫废水电渗析软化浓缩处理系统，其特征在于，所述加药装置(12)内装有盐酸。
4.一种火电厂脱硫废水电渗析软化浓缩处理方法，其特征在于，基于权利要求3所述的火电厂脱硫废水电渗析软化浓缩处理系统，包括以下步骤: 1)火电厂产生的脱硫废水进入原水池(I)中，原水池(I)中的脱硫废水进入到第一反应池(2)中，同时氢氧化钠储罐(3)中的氢氧化钠进入第一反应池(2)中，使第一反应池(2)中脱硫废水的pH值调整至10-11 ;经第一反应池(2)处理后的脱硫废水与混凝剂储罐(5)输出的混凝剂及助凝剂储罐(6)中的助凝剂混合后输入到第一澄清器(4)中，并在第一澄清器(4)混凝沉淀，进而去除脱硫废水中Mg2+以及部分重金属离子； 2)经第一澄清器(4)处理后的脱硫废水进入到第二反应池(7)中，并与纯碱储罐(8)输出的纯碱在第二反应池(7)中进行反应，使脱硫废水中的Ca2+生成CaCO3，并去除剩余的重金属离子，同时经第二反应池(7)处理后的脱硫废水进入到第二澄清器(9)中，并在第二澄清器(9)中进行沉淀，经在第二澄清器(9)中沉淀的脱硫废水进入到中间水池(10)中； 3)中间水池(10)中的脱硫废水与加药装置(12)中输出的盐酸进行混合后，使脱硫废水的PH值调整至9-10，然后进入到电渗析装置(11)，并经电渗析装置(11)分离为淡水及浓缩水，其中淡水进入到淡水池(14)中回收利用，浓缩水经蒸发结晶系统(16)蒸发结晶并回收。
5.根据权利要求4所述的火电厂脱硫废水电渗析软化浓缩处理方法，其特征在于，进入到第二反应池(7)中的脱硫废水中Ca2+的摩尔质量与进入到第二反应池(7)中纯碱的摩尔质量的比例为1:1。
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