CN103319042B - 高盐复杂废水回用与零排放集成设备及工艺 - Google Patents
高盐复杂废水回用与零排放集成设备及工艺 Download PDFInfo
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- CN103319042B CN103319042B CN201310298389.8A CN201310298389A CN103319042B CN 103319042 B CN103319042 B CN 103319042B CN 201310298389 A CN201310298389 A CN 201310298389A CN 103319042 B CN103319042 B CN 103319042B
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- Prior art keywords
- salt
- concentrated
- pressure
- water
- film
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- 239000011780 sodium chloride Substances 0.000 title claims abstract description 80
- 239000002351 wastewater Substances 0.000 title claims abstract description 47
- 238000005516 engineering processes Methods 0.000 title abstract description 10
- 239000011901 water Substances 0.000 claims abstract description 106
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 38
- 238000002425 crystallisation Methods 0.000 claims abstract description 21
- 238000001704 evaporation Methods 0.000 claims abstract description 19
- 238000001471 micro-filtration Methods 0.000 claims abstract description 19
- 238000000034 methods Methods 0.000 claims abstract description 18
- 238000005345 coagulation Methods 0.000 claims abstract description 17
- 230000015271 coagulation Effects 0.000 claims abstract description 17
- 238000000889 atomisation Methods 0.000 claims abstract description 12
- 238000010612 desalination reactions Methods 0.000 claims abstract description 11
- 241000563946 Paracryphiaceae Species 0.000 claims abstract description 8
- 206010042602 Supraventricular extrasystoles Diseases 0.000 claims abstract description 8
- 229920002401 polyacrylamides Polymers 0.000 claims abstract description 8
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Chemical compound 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[Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 8
- 239000011649 sodium carbonate Substances 0.000 claims abstract description 8
- 229910000029 sodium carbonate Inorganic materials 0.000 claims abstract description 8
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- 238000006065 biodegradation reactions Methods 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N calcium Chemical compound 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[Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
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- 239000011575 calcium Substances 0.000 description 1
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- FYYHWMGAXLPEAU-UHFFFAOYSA-N magnesium Chemical compound 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[Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910001425 magnesium ion Inorganic materials 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 238000001728 nano-filtration Methods 0.000 description 1
- 239000011368 organic materials Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
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- CBENFWSGALASAD-UHFFFAOYSA-N ozone Chemical compound 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Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Abstract
Description
技术领域
[0001] 本发明涉及一种高盐复杂废水的综合处理设备及工艺,是一种针对工业反渗透浓水和高含盐量、高有机物含量复杂废水的回用与零排放的多元化设备集成系统。
背景技术
[0002] 近年来,在电力、冶金、炼油、煤化工等工业生产过程中产生的废水及循环冷却排污水等问题越来越受到重视。随着水资源成本的不断提高,和国家对企业污水排放控制力度的加大,污水回用技术得到了广泛的普及。在此过程中,反渗透膜技术(RO)已经逐渐成为工业循环水处理、废水回用和海水淡化领域中的重要手段。
[0003] 但采用反渗透技术仍存在两个问题:一是反渗透技术的高脱盐率,一般情况下反渗透装置可稳定的脱盐率水平在98%以上,即98% 以上的盐分进入反渗透浓水中;二是水回收利用率低,一般只能达到70%-80%,仍有20%-30%左右浓水排放,排放量大,造成了水资源的巨大浪费。同时,产生的高盐复杂废水中含有大量的溶解性盐类,其中包括大量钙、镁结垢离子,重金属离子,硅离子以及其它盐类,并且通常还会含有大量不可生化降解的有机污染物,目前的处理方法都是采用简单处理后,直接排放,对地表水环境造成了严重的影响。
[0004]目前,针对反渗透浓水以及类似的高盐复杂废水的处理,主要有以下几种方案:第一,采用臭氧、二氧化氯、芬顿试剂等强氧化物质进行催化氧化,然后进入生化单元去除或部分去除废水中的有机物,然后经沉淀或过滤后直接排放;第二,将高盐水通过离子交换或投加药剂控制钙镁离子的沉淀,通过二次反渗透装置回收部分水资源,再次产生的浓水直接排放;第三,将浓水进行蒸发和结晶,实现真正的零排放。
[0005] 综合分析以上三种方案,第一种方案只针对废水中的有机物进行处理,然而,一般的污水处理都是经过很长流程的生化处理,所余部分有机物可生化性极差,甚至不可生化,因此,单靠化学催化氧化对该部分的去除效果是非常有限的,最主要的是对废水的高盐组分并无去除效果,而且高浓度的盐分会降低生化的运行效果;第二种方案尽管从理论上存在其合理性,然而,反渗透浓水是已经将原水进行了至少4倍浓缩后的高含盐废水,所有的钙镁等结垢离子、重金属离子、硅离子等,以及不可生化有机物等污染物质浓度已经很高,因此,普通的反渗透膜对该废水的回收率是极低的,甚至海水淡化膜也只能做到40~55%,所剩余的浓水量还是比较大的;第三种方案,对高盐废水处理得最彻底,相对技术也最成熟,缺点是处理成本太高,过程中需要大量蒸汽,平均吨水处理成本在几十元以上,无法针对大水量高盐水进行处理,并且,蒸发结晶反应设备对材质要求较高,导致一次性投资太大。
发明内容
[0006] 本发明的目的是克服上述不足,而提供一种高盐复杂废水回用与零排放集成设备及工艺,解决现有技术中存在的以上问题。
[0007] 本发明采取的技术方案为:
[0008] 高盐复杂废水回用与零排放集成设备,包括预处理系统、回用与减量化系统、零排放系统,预处理系统包括调节池,调节池通过提升泵连接混凝反应池,混凝反应池连接浸没式微滤池,浸没式微滤池的上部与回用与减量化系统连接,底部与污泥池连接;所述的回用与减量化系统包括与浸没式微滤池连接的中间水池,中间水池通过增压泵、保安滤器与中压浓缩膜装置连接,中压浓缩膜装置连接中压浓水池,中压浓水池通过增压泵、保安滤器与高压浓缩膜装置连接,高压浓缩膜装置通过段间增压泵与超高压浓缩膜装置连接,超高压浓缩膜装置通过浓缩盐水箱与零排放系统连接;零排放系统包括与浓缩盐水箱相连的增强雾化蒸发机、蒸发结晶装置,增强雾化蒸发机与蒸发塘相通,蒸发塘连接干盐处置装置,蒸发结晶装置通过盐泥脱水装置与干盐处理装置连接。
[0009] 所述的混凝反应池、中压浓缩膜装置、高压浓缩膜装置、超高压浓缩膜装置上均设有加药装置。
[0010] 所述的中压浓缩膜装置、高压浓缩膜装置、超高压浓缩膜装置、蒸发结晶装置均连有回用水箱。所述的浓缩膜为特种膜,膜片耐高压,根据不同的浓度,耐压50bar/80bar/160bar ;耐高污染,根据COD组成不同,可能高达数百、数千或数万ppm。浓缩膜可以是主要截留二价以上离子的纳滤或能够对所有离子截留率都很高的反渗透级别。
[0011] 高盐复杂废水回用与零排放集成工艺,步骤为:
[0012] (I)将高盐复杂废水进行均质和均量处理,然后依次加入氢氧化钠、碳酸钠、PAC、PAM进行混凝处理,混凝处理后的混合液进入滤池用浸没式微滤膜沉降过滤,沉降2-5小时后,污泥从底部排出,上清液进入反渗透处理工序;
[0013] (2)反渗透处理工序为先在2.0-3.5Mpa下用中压膜元件脱盐浓缩,然后再用高压膜元件在3.5-4.5Mpa进一步脱盐浓缩,再在12.0-16.0Mpa用超高压膜元件进一步脱盐浓缩;反渗透处理得到的纯水进入回用水箱利用,浓缩盐水进一步处理;
[0014] (3)浓缩盐水经结晶处理,排放的盐泥经盐泥脱水,最终得到固体盐作为固体废弃物干盐处置;或者浓缩盐水排放到蒸发塘,雾化蒸发处理,得到固体盐作为固体废弃物干盐处置。
[0015] 上述方法中,步骤(1)氢氧化钠配制成5_20wt%浓度的溶液,按照1.5g/L高盐复杂废水的浓度投加量;碳酸钠配制成5-15wt%浓度的溶液,按照3.2g/L高盐复杂废水的浓度投加量;PAC配成5-20wt%浓度的溶液,按照30mg/L高盐复杂废水的浓度投加量加入,PAM配成0.1-0.3%浓度的溶液按照3mg/L高盐复杂废水的量加入。
[0016] 预处理部分,通过调节池将高盐复杂废水进行均质和均量,通过提升泵将原水送到混凝反应池,在此从加药装置依次加入石灰或氢氧化钠、碳酸钠、PAC、PAM,混合液体进入浸没式微滤池,在自然沉降作用下,上清液通过浸没式微滤管收集后进入中间水池,化学污泥通过重力沉降从底部排入污泥池,经过污泥调整后进入污泥脱水设备进行泥水分离,成为泥饼后的干污泥最终进行干污泥处置。在预处理后脱除水中的硬度及易结垢离子和部分COD后,经中间水池收集,利用增压泵提升料液压力依次通过保安滤器、中压浓缩膜装置,中压浓缩膜装置采用特种浓缩抗污染中压膜元件GTR3-8040F-65(流道宽度65mil),约70%原水以上的产水进入回用水箱,约30%原水的反渗透浓液进入中压浓水池。中压浓水池通过增压泵提升浓水作为高压浓缩膜装置的进水,高压浓缩膜装置前设置保安滤器,高压浓缩膜装置用特种浓缩抗污染高压膜元件GTR4-8040F-80(流道宽度80mil),约65%进水以上的产水进入回用水箱,约35%进水的反渗透浓水通过段间增压泵增压后作为后续超高压浓缩膜装置的进水,超高压浓缩膜采用超高压DTRO碟管式膜元件7W101500 (流道宽度6mm),约55%进水以上的产水进入回用水箱,约45%进水的反渗透浓水进入浓缩盐水箱。通过本装置回用与减量化部分,约可回收95%以上优质脱盐水回用于生产装置,最终浓缩后的低于5%的浓缩盐水进行零排放处理。零排放部分,根据冬季与夏季的气候条件分别运行,降低运行费用。在冬季,通过成熟技术多效蒸发结晶装置和盐泥脱水,将总量不足5%原水的浓缩盐水转化为蒸馏水和固态盐,蒸馏水返回回用水箱,固态盐进而进行干盐处置;在夏季,充分利用自然条件的便利,通过增强雾化蒸发机,将浓缩盐水雾化并吹散到空中,利用自然光照和风力强化蒸发效果,该设备比传统自然蒸发增强效果14~35倍,但需与蒸发塘组合使用,散落的干盐经收集后,进行干盐处置。本发明可将反渗透浓水或类似高盐复杂废水回收95%以上重新利用,只留5%左右的高浓盐水进入蒸发结晶,或进入自然蒸发塘,充分循环利用水资源,降低高盐复杂废水的回用与零排放的成本。
[0017] 本发明的基本原理如下:
[0018] 1、本发明采用化学方法将重金属离子、钙镁等硬度离子在进入浓水反渗透之前除去,同时部分地将C0D、有 机胶体物质通过混凝、吸附的作用降低浓度,然后再进入反渗透系统,这样,反渗透膜表面就避免了重金属污染和钙镁结垢的倾向;
[0019] 2、本发明采用浸没式微滤装置作为反渗透进水预过滤单元,通过孔径为1-5微米的PE微滤管,将化学沉淀、混凝胶体物质等进一步得到去除,使前段预处理即达到符合后续RO进水的SDI指标,同时又降低了对后续RO产生污堵的有机、无机物质,使整个系统更趋于合理,保证系统长期、稳定、可靠运行。
[0020] 3、一般高盐复杂废水来源为反渗透浓水,为浓缩4倍原水后的废水,其不可生化降低的COD以及易结垢的硅离子均较高,经本发明设备再浓缩10-20倍后,其浓度将更大,更易在反渗透浓水侧形成有机污染和硅结垢,在本发明技术中,在预处理部分通过混凝、吸附作用可部分地降低COD和硅离子,同时,保持反渗透的进水PH值在8.0-11.0,碱性条件下也抑制了膜表面硅结垢和有机污染的倾向。
[0021] 4、本发明中的中压浓缩膜装置采用流道宽度为65mil (约1.65mm)的特种浓缩抗污染中压膜元件,高压浓缩膜装置采用流道宽度为SOmil (约2.03mm)的特种浓缩抗污染高压膜元件,超高压浓缩膜装置采用流道宽度为6mm的DTRO超高压膜元件。与传统抗污染高流量的膜元件最大流道宽度34mil (约0.86mm)相比,本发明采用的中、高、超高压膜元件具有超大流道的特点,特殊的流道和结构设计,使浓缩膜系统更不易发生离子结垢和有机物的污堵。
[0022] 5、本发明针对的高含盐复杂废水一般来自浓缩4倍的反渗透浓水或者其它高含盐量的生产废水,其含盐量一般介于4000-7000mg/L,通过本装置系统视冬季和夏季运行情况,可将系统回收率达到95-99.5%。
[0023] 为了更清楚表达本发明所达到的技术效果,将进水指标及出水指标列表说明。
[0024]
[0025] 本发明集成设备具有技术成熟、工程投资低、运行费用少、操作管理简单、系统运行稳定可靠、占地面积省等特点,回收产品水水质优良,可用于循环水补充水或脱盐水站补充水。适用于电力、冶金、炼油、煤化工等工业生产过程中产生的反渗透浓水及循环冷却排污水的处理,除回收优质水外,可实现真正意义上的、企业用得起的零排放,能为水资源较为紧张的地区(如新疆、内蒙、宁夏、陕西、山西等)引进需要消耗大量水资源的企业,开创了一条水资源循环利用的新道路。
[0026] 本发明集成设备改变了现有技术中直接将反渗透浓水等高盐复杂废水直接进行蒸发浓缩的工艺,创造性地利用新型特种抗污染高压浓缩膜对高盐复杂废水进行进一步的减量化,在普通反渗透浓缩4倍后的浓水及同等水平含盐量的高盐水基础上,再次浓缩减量,通过本发明设备后,可回收95%以上优质水,使得高盐水最终浓缩液体只有进水的5%左右。这样便大大降低了进入蒸发结晶部分的水量,便工程投资大幅降低,运行费用减少4倍以上。本发明集成设备回收的95%以上优质水可回用于循环水、绿化等用途,减少新鲜水用量,5%的浓缩液体进入蒸发结晶,减小了蒸发结晶装置的投资规模,降低了蒸汽等能源消耗。因此,从工程建设投资到运行维护费用,均得到了绝对的降低。
附图说明
[0027] 图1是本发明的工艺流程示意图;
[0028] 图2为本发明高盐复杂废水回用与零排放集成设备结构图;
[0029] 其中1.高含盐废水,2.调节池,3.提升泵,4.混凝反应池,5.浸没式微滤池,6.污泥池,7.污泥脱水设备,8.干污泥处理,9.中间水池,10.增压泵,11.保安滤器,12.中压浓缩膜装置,13.中压浓水池,14.增压泵,15.保安滤器,16.高压浓缩膜装置,17.段间增压泵,18.超高压浓缩膜装置,19.浓缩盐水箱,20.增强雾化蒸发机,21.蒸发塘,22.蒸发结晶装置,23.盐泥脱水装置,24.干盐处置装置,25.回用水箱,26.回用水泵,27.用户,28.加药装置,29.加药装置。
具体实施方式
[0030] 下面结合附图和实施例对本发明进行进一步的阐述。
[0031 ] 如图2所示,高盐复杂废水回用与零排放集成设备,包括预处理系统、回用与减量化系统、零排放系统,预处理系统包括调节池2,调节池2通过提升泵3连接混凝反应池4,混凝反应池4连接浸没式微滤池5,浸没式微滤池5的上部与回用与减量化系统连接,底部与污泥池6连接;所述的回用与减量化系统包括与浸没式微滤池5连接的中间水池9,中间水池9通过增压泵10、保安滤器11与中压浓缩膜装置12连接,中压浓缩膜装置12连接中压浓水池13,中压浓水池13通过增压泵14、保安滤器15与高压浓缩膜装置16连接,高压浓缩膜装置16通过段间增压泵17与超高压浓缩膜装置18连接,超高压浓缩膜装置18通过浓缩盐水箱19与零排放系统连接;零排放系统包括与浓缩盐水箱19相连的增强雾化蒸发机20、蒸发结晶装置22,增强雾化蒸发机20与蒸发塘21相通,蒸发塘21连接干盐处置装置24,蒸发结晶装置22通过盐泥脱水装置23与干盐处理装置24连接。
[0032] 所述的混凝反应池4、中压浓缩膜装置12、高压浓缩膜装置16、超高压浓缩膜装置18上均设有加药装置。
[0033] 所述的中压浓缩膜装置12、高压浓缩膜装置16、超高压浓缩膜装置18、蒸发结晶装置22均连有回用水箱25。
[0034] 实施例1:
[0035] 如图1所示,应用本集成设备处理煤化工高含盐复杂废水,废水来自污水回用反渗透浓水及脱盐水站反渗透浓水。
[0036] 首先,通过调节池将高盐复杂废水进行均质和均量,通过提升泵将原水送到混凝反应池,在此从加药装置依次加入石灰或氢氧化钠、碳酸钠、PAC、PAM。氢氧化钠配制成20%浓度的溶液按照1.5g /L的原水浓度投加量,碳酸钠配制成15%浓度的溶液按照3.2g/L的原水浓度投加量,PAC配成20%浓度的溶液按照30mg/L的浓度投加量加入,PAM配成0.3%浓度的溶液按照3mg/L的量加入,加药量不宜过大,应根据进水各离子浓度变化情况进行调整,否则会造成膜污染,影响膜的使用寿命。
[0037] 混合液体进入浸没式微滤池,滤池总水力停留时间为2.5h,在自然沉降作用下,上清液通过浸没式微滤管收集后进入中间水池,化学污泥通过重力沉降从底部排入污泥池,经过污泥调整后进入污泥脱水设备7进行泥水分离,成为泥饼后的干污泥最终进行干污泥处置。浸没式微滤膜采用某国产亲水PTFE管式膜,能处理高含固量物质,高浓度液流,能有效地控制浓差极化和污垢,延长了膜清洗的周期。并且PTFE的高耐化学性的优点,可以使用浓碱液直接进行浸泡清洗。
[0038] 中压浓缩膜装置采用膜材质为芳香族聚酰胺复合材料,操作压力为2.0-3.5Mpa,回收率大于70%,能截留97.5%的盐类物质,可将平均TDS为6500mg/L的原水浓缩到TDS大于21600mg/L,占总处理量30%的浓水进入到高压浓缩膜装置进行进一步脱盐浓缩;高压浓缩膜装置膜材质为芳香族聚酰胺复合材料,操作压力为3.5~4.5Mpa,回收率大于65%,能截留97.2%以上的盐类物质,可将平均TDS为21600mg/L的原水浓缩到TDS大于51700mg/L,占总处理量10.5%的浓缩液进入到超高压浓缩膜装置进行进一步脱盐浓缩;超高压浓缩膜装置膜材质为芳香族聚酰胺复合材料,操作压力为12.0-16.0Mpa,回收率大于55%,能截留96.2%以上的盐类物质,可将平均TDS为51700mg/L的原水浓缩到TDS大于105000mg/L,占总处理量4.7%的浓缩液进入后续零排放单元。
[0039] 经过预处理+反渗透的高浓缩含盐水经过热交换器加热后进入蒸发结晶装置,产生的蒸汽被送到冷凝器冷凝成纯净水送到回用水箱。从结晶器排放的盐泥经盐泥脱水,最终得到固体盐作为固体废弃物干盐处置。当夏季时,浓缩盐水可排放到蒸发塘,靠增强雾化蒸发机利用当地光照好、空气湿度小的便利条件,进行强化蒸发,使零排放的运行成本会明显下降。
[0040] 上述虽然结合图1对本发明的具体实施方式进行了描述,但并非对本发明保护范围的限制,在本发明的技术方案的基础上,本领域技术人员不需要付出创造性劳动即可做出的各种修改或变形 仍在本发明的保护范围以内。
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