CN108275815A - 一种高盐废水零排放蒸发结晶盐分质系统及方法 - Google Patents
一种高盐废水零排放蒸发结晶盐分质系统及方法 Download PDFInfo
- Publication number
- CN108275815A CN108275815A CN201711427252.2A CN201711427252A CN108275815A CN 108275815 A CN108275815 A CN 108275815A CN 201711427252 A CN201711427252 A CN 201711427252A CN 108275815 A CN108275815 A CN 108275815A
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- Prior art keywords
- nitre
- crystallization
- salt
- evaporated
- freezing
- Prior art date
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- 239000011780 sodium chloride Substances 0.000 title claims abstract description 189
- 150000003839 salts Chemical class 0.000 title claims abstract description 159
- 238000001704 evaporation Methods 0.000 title claims abstract description 45
- 239000002351 wastewater Substances 0.000 title claims abstract description 41
- FGIUAXJPYTZDNR-UHFFFAOYSA-N Potassium nitrate Chemical compound 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h0Pgo8L3N2Zz4K [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 claims abstract description 272
- 238000002425 crystallisation Methods 0.000 claims abstract description 255
- 230000005712 crystallization Effects 0.000 claims abstract description 255
- 238000007710 freezing Methods 0.000 claims abstract description 88
- 238000007906 compression Methods 0.000 claims abstract description 69
- PMZURENOXWZQFD-UHFFFAOYSA-L na2so4 Chemical compound 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[Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims abstract description 52
- 239000000498 cooling water Substances 0.000 claims abstract description 32
- 229910052938 sodium sulfate Inorganic materials 0.000 claims abstract description 30
- 235000011152 sodium sulphate Nutrition 0.000 claims abstract description 30
- 239000012452 mother liquor Substances 0.000 claims description 70
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- 239000010842 industrial wastewater Substances 0.000 description 5
- FYYHWMGAXLPEAU-UHFFFAOYSA-N magnesium Chemical compound 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[Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 5
- 229910052749 magnesium Inorganic materials 0.000 description 5
- 239000011777 magnesium Substances 0.000 description 5
- 239000000155 melt Substances 0.000 description 5
- 239000002699 waste material Substances 0.000 description 5
- OYPRJOBELJOOCE-UHFFFAOYSA-N calcium Chemical compound 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[Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 4
- 229910052791 calcium Inorganic materials 0.000 description 4
- 239000011575 calcium Substances 0.000 description 4
- 238000005345 coagulation Methods 0.000 description 4
- 230000015271 coagulation Effects 0.000 description 4
- 235000019628 coolness Nutrition 0.000 description 4
- 238000001764 infiltration Methods 0.000 description 4
- 239000011347 resin Substances 0.000 description 4
- 229920005989 resin Polymers 0.000 description 4
- 239000010802 sludge Substances 0.000 description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Chemical compound 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[Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 4
- 241000276438 Gadus morhua Species 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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[S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
- 239000010414 supernatant solution Substances 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
- C01D3/06—Preparation by working up brines; seawater or spent lyes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
-
- 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
-
- 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
- C02F1/22—Treatment of water, waste water, or sewage by freezing
-
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/281—Treatment of water, waste water, or sewage by sorption using inorganic sorbents
-
- 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
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- 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
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- 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
-
- 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
-
- 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
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- 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
- C02F2001/5218—Crystallization
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
Abstract
本发明涉及一种盐分质系统及方法,该系统用于对高盐废水进行蒸发结晶,所述系统包括硝蒸发结晶装置(13)、冷冻硝结晶装置(20)和盐蒸发结晶装置(27),其中,所述硝蒸发结晶装置(13)和所述盐蒸发结晶装置(27)在分别利用第一蒸汽压缩机(16)和第二蒸汽压缩机(31)抽取并压缩二次蒸汽的条件下参照冷冻硝结晶所需温度通过所述第一蒸汽压缩机(16)和所述第二蒸汽压缩机(31)连接冷却水系统(35)并利用冷却器(37)和/或冷冻机(36)保持所述冷冻硝结晶装置(20)内部所需温度。本发明的高盐废水零排放蒸发结晶盐分质方法分离出的硫酸钠及商业盐作为工业可回收原料加以利用,重复利用水资源,达到污水低成本零排放,防止污水排放对环境造成的不利影响。
Description
一种高盐废水零排放蒸发结晶盐分质系统及方法
[0001] 本发明是原申请号为2〇1510981747.4,原发明名称为:一种高盐废水零排放蒸发 结晶盐分质方法的分案申请。
技术领域
[0002] 本发明涉及节能减排技术领域,尤其涉及一种高盐废水零排放蒸发结晶分质方法 和系统。
背景技术
[0003] 近年来,随着石化、电力、冶金、煤化工等行业的快速发展,工业生产过程中产生的 反渗透浓水、工业污水、循环排污水及部分工艺排水等含成分较复杂的污水量逐年增加,这 些成分复杂的污水如何最终处置和再利用问题受到广泛的重视。随着国家对企业污水排放 控制力度日趋严格,特别是在水资源匮乏地区,如何合理处置利用好这部分含成分复杂的 污水,实现废水零排放,对保护我们赖以生存的周边环境和自然水体,进一步提高水资源的 综合利用效率,缓解水资源紧张状况具有重要意义,目前污水处理回用在诸多废水处理技 术中,利用反渗透膜法处理技术应用已经逐渐成为工业循环水处理污、废水回用、减量化等 领域中的一种非常重要处理手段。
[0004] 目前,针对高浓度盐且含难降解有机物废水的处理方法,主要有以下几种方案:
[0005] 第一,对废水中的难降解有机物类物质采用强氧化性物质(主要有臭氧、双氧水 等)进行催化氧化,使废水中难降解的有机物类物质进行有效降解,经氧化处理后的废水再 进入生化单元对污水中的有机物进行去除,经过沉淀和过滤单元后直接排放;
[0006]第二,将含钙镁硬度废水通过软化后,再通过二次反渗透装置进行减量处理进一 步回收部分水量,减量化后产生的浓水直接排放;
[0007]第三,减量化后的高含盐浓水零排处置是高盐浓水利用多蒸发和结晶单元进行处 理,形成混盐类,实现水的零排放。
[0008]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有效处理消化, 一般的污水处理都是经过较长的生化处理流程,废水中剩余部分有机物可生化性极差,甚 至不能生化,因此,单靠化学催化氧化对该部分的去除效果是有限的,最主要的是上述方法 对废水中无机盐成分基本无去除作用;第二种方案尽管从工艺上对原水进行一定减量处 理,然而,反渗透浓水已经是将原水进行了至少4倍浓缩后的高盐废水,所有的钙离子、镁离 子、重金属离子、硅离子等,以及不可生化的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不高,甚至海水淡化膜也只能回收50%左右,所产生的浓水虽 然进行减量但是产生的浓水水量还是比较大,仍然有占总处理水10%以上的较浓盐水对环 境产生很大影响;第三种方案,对浓缩后高盐废水处理得较彻底,相对技术成熟,只是处理 成本太高,过程中需要消耗大量蒸汽,根据最终浓水含盐浓度一般水处理成本在50元/吨以 上,而且一般只分离一种盐或直接形成混盐,混盐作为危废物需要进行特殊处理,成本很 高,该法对大量高盐水进行处理其投资费用及运行成本都非常高。
[0009] 中国专利CN103508602B公开了一种膜与蒸发结晶集成的高盐度工业废水零排放 的工艺,具体公开了将工业废水经超滤预处理后经过高压杲输送至反渗透过程,渗透测出 水回用,对过滤多次后的浓缩液进行电渗析处理,经电渗析浓缩后的物料进行蒸发和结晶, 得到盐泥和冷凝水。上述发明将膜与蒸发结晶耦合不仅能从高盐浓度的工业废水中回收高 质量的净水,也能实现高盐废水的零排放,但是上述发明的物料经最后的蒸发结晶后只能 得到盐泥的混合物,并且对于最终得到的盐泥也无法得到充分再利用,工业废水经超滤预 处理并经过反渗透和电渗析处理后得到的高浓度盐浓缩液中含有多种成分,包括氯化钠硫 酸钠等,直接放弃或排放会造成很大的浪费,形成的固危废也会对环境产生一定污染。
发明内容
[0010] 针对现有技术之不足,本发明提供了 一种高盐废水零排放蒸发结晶盐分质方法。本发 明通过将工业污水、废水经预处理、反渗透得到的含盐浓水回收95 %以上水量重新利用,剩余 5%左右水量的较高浓盐水通过电驱动离子膜进行处理,进一步深度浓缩成比例达1〇%-12% 的浓盐水,再进一步对高盐水深度浓缩达20 %的浓盐液,经过硝蒸发结晶单元、盐蒸发结晶单 元,分别结晶析出硫酸钠和氯化钠等分质盐。作为工业可回收原料加以利用变废为宝,充分重 复利用水资源,达到污水低成本零排放,实现综合利用防止污水排放对环境造成的不利影响。
[0011] 本发明提供了一种高盐废水零排放蒸发结晶盐分质方法,所述方法包括经预处理 及减量化浓缩后的高浓度盐浓缩液依次通过硝蒸发结晶装置、冷冻硝结晶装置和盐蒸发结 晶装置按照硫酸钠、氯化钠的分离顺序进行分质,所述硝蒸发结晶装置和所述盐蒸发结晶 装置在分别利用第一蒸汽压缩机和第二蒸汽压缩机抽取并压缩二次蒸汽的条件下参照冷 冻硝结晶所需温度通过所述第一蒸汽压缩机和所述第二蒸汽压缩机连接冷却水系统并利 用冷却器和/或冷冻机保持所述冷冻硝结晶装置内部所需温度。
[0012]根据一个优选实施方式,所述分质方法还包括如下步骤:
[0013] 将所述高浓度盐浓缩液在负压或微正压下由所述硝蒸发结晶装置进行蒸发结晶;
[0014] 经蒸发结晶产生的硝母液经所述冷冻硝结晶装置冷冻结晶,经所述冷冻硝结晶装 置产生的混合物通过冷冻硝离心分离器离心分离,离心产生的晶体再次返回与经所述硝蒸 发结晶装置产生的硝液热融混合后再经离心分离器分离出硫酸钠晶体;
[0015] 经所述冷冻硝离心分离器离心产生的冷冻硝母液经冷硝母液泵加入所述盐蒸发 结晶装置并在负压下蒸发结晶得盐;
[0016] 由所述硝蒸发结晶装置和所述盐蒸发结晶装置蒸发产生的二次蒸汽分别通过第 一蒸汽压缩机和第二蒸汽压缩机抽取并分别由第一加热器和第二加热器提高温度后持续 为所述硝蒸发结晶装置和所述盐蒸发结晶装置中的浓缩液提供热能。
[0017] 根据一个优选实施方式,所述硝蒸发结晶装置和所述盐蒸发结晶装置蒸发产生的 二次蒸汽分别通过所述第一蒸汽压缩机和所述第二蒸汽压缩机连接冷却水系统并通过冷 冻机为所述第一蒸汽压缩机和所述第二蒸汽压缩机提供循环冷却水,同时所述冷冻机连接 冷却器并通过冷硝循环泵保持所述冷冻硝结晶装置维持在一 6〜一 5°c。
[0018] 根据一个优选实施方式,所述高浓度盐浓缩液在进行分质前,由含有复杂成分的 废水依次经过预处理部分、回用与减量化部分后形成减量浓缩后的高浓度盐浓缩液。
[0019] 根据一个优选实施方式,所述高浓度盐浓缩液通过增压栗进入原料进料预热器预 热后经所述繼雜0¾雜贿倾雜賴織结帛,臓臟雜n體纟别肖循环栗 连接所述第一加热器对所述硝蒸发结晶装置循环加热;所述硝蒸发结晶装置通过接连真空 系统使所述硝蒸发结晶装置保持负压或不采用真空系统保持微正压状态。
[0020]根据一个优^施方式,所述硝蒸发结晶装置在负压或微正压状态下,持续进行 水分蒸发浓缩,所述硝蒸发结晶装置内高盐浓缩液的温度维持在100〜115 °C。
[0021]根据一个优选实施方式,所述高浓度盐浓缩液经所述硝蒸发结晶装置蒸发结晶后 进入硝稠厚器进行调整后进入离心分离装置,经离心后的硫酸钠晶体经烘干设备干燥后, 进行计量包装得到商品硫酸钠。
[0022]根据一个优选实施方式,所述离心分离装置中产生的硝母液进入硝母液槽,并经 硝母液栗进入所述冷冻硝结晶装置进行降温结晶。
[0023]根据一个优选实施方式,所述硝母液在所述冷冻硝结晶装置中进行结晶后排放至 沉降器后进行调整,所述冷冻硝结晶装置连接冷却器并通过冷硝循环泵使所述冷冻硝结晶 装置保持在一 6 5°C,
[0024]所述冷冻硝母液通过冷冻硝母液泵进入预热器进行加热,然后进入所述盐蒸发结 晶装置并在负压下进行蒸发结晶;
[0025]所述盐蒸发结晶装置通过循环栗连接第二加热器对所述盐蒸发结晶装置进行加 热,所述盐蒸发结晶装置产生的二次蒸汽通过所述第二蒸汽压缩机抽取并经第二加热器提 高温度后用于所述预热器内部液体的加热。
[0026] 所述经盐蒸发结晶后的产物通过稠厚器进入盐离心分离器分离后,再将晶体经烘 干得到商品盐。
[0027] 根据本发明的另一个方面,本发明还提供了一种用于高盐废水零排放蒸发结晶分 质方法的装置,所述装置包括:增压泵,所述增压泵连接原料进料预热器的第一进口;所述 原料进料预热器的出料口连接硝蒸发结晶装置的第一进口,所述硝蒸发结晶装置的第一出 口连接第一蒸汽压缩机的第一进口,所述硝蒸发结晶装置的第二出口连接硝循环泵的进 口,所述硝循环栗的出口连接第一加热器的第一进口;所述第一蒸汽压缩机的第一出口连 接第一加热器的第二进口,所述第一加热器的第一出口连接所述原料进料预热器的第二进 口,所述第一加热器的第二出口连接硝蒸发结晶装置的第二进口,所述第一蒸汽压缩机的 第二出口连接冷却水系统的第一进口,所述硝蒸发结晶装置的第三出口连接真空系统的第 一进口;所述硝蒸发结晶装置的第四出口连接硝稠厚器的进料口;所述硝稠厚器的出料口 连接离心分离器的进料口;所述离心分离器的第一出口连接硝母液槽的进料口,所述离心 分离器的第二出口连接烘干装置的进口;所述硝母液槽的出料口连接硝母液栗的进料口’ 所述硝母液栗的出料口连接冷冻硝结晶装置的第一进口,所述冷冻硝结晶装置的第二出口 连接沉降器的进料口,所述冷冻硝结晶装置的第二出口连接冷却器的第—进口,所述^却 器的第一出口连接冷冻机的第一进口,所述冷冻机的第一出口连接冷却水系统的第二进 口,所述冷却器的第二出口连接冷硝循环栗的进口,所述冷硝循环泵的出口连接所述冷冻 硝结晶装置的第二进口;所述沉降器的出料口连接冷冻硝离心分离器的进料口:所述冷冻 硝离心分离器的第一出口连接冷冻硝母液槽的进料口,所述冷冻硝分离器的第二出口连接 所述硝稠厚器的进料口;所述冷冻硝母液槽的出料口连接冷硝母液栗的进料口,所述冷硝 母液泵的出料口连接预热器的第一进口,所述预热器的出料口连接盐蒸发结晶装置的第一 进口;所述盐蒸发结晶装置的第一出口连接循环栗的进口,所述盐蒸发结0曰連置的弟一出 口连接稠厚器的进料口,所述盐蒸发结晶装置的第三出口连接真空系统的第二进口;所述 循环栗的出口连接第二加热器的第一进口,所述第二加热器的第一出口连接所述盐蒸^结 晶装置的第二进口,所述第二加热器的第二出口连接所述预热器的第二进口;所述盐蒸发 结晶装置的第四出口连接第二蒸汽压缩机的第一进口,所述第二蒸汽压缩机的第一出口^ 接所述第二加热器的第二进口,所述第二蒸汽压缩机的第二出口连接所述冷却水系统的第 三进口,所述冷却水系统的第一出口连接所述第一蒸汽压缩机的第二进口,所述冷却水系 统的第二出口连接所述第二蒸汽压缩机的第二进口,所述冷却水系统的第三出口连接所述 冷冻机的第二进口,所述冷冻机的第二出口连接所述冷却器的第二进口;所述稠厚器的出 料口连接盐离心分离器的进料口,所述盐离心分离器的出料口连接烘干装置的进口。
[0028] 本发明的有益技术效果在于:
[0029] 1、本发明采用化学方法先将污水中的重金属离子、钙镁等硬度离子有效去除,同 时也去除了大部分的C0D有机胶体物质等,防止料液在进入反渗透系统后对反渗透膜表面 造成有机物污染以及由于钙镁结垢的堵塞问题。
[0030] 2、本发明通过采用管式微滤装置和树脂作为反渗透单元,将化学反应生成的沉淀 物、混凝物胶体物质等进一步去除,分别再通过中压反渗透、高压反渗透减量化浓缩液使 TDS达到约50000mg/L,使系统回收率达到85%左右。通过两级电驱动离子膜进一步浓缩使 得整个工艺流程达到回收水量95 %以上,TDS约为200000mg/L。
[0031] 3、本发明通过将经预处理和深度浓缩产生的浓盐液经过蒸发结晶后得到部分硫 酸钠,然后又进一步通过冷冻硝结晶装置低温结晶得到固体结晶芒硝,产生的芒硝再次返 回与硝蒸发结晶装置产生的热融液混合循环处理,充分析出浓盐液中的硫酸钠晶体。浓缩 液经分离出硫酸钠后再通过盐蒸发结晶装置进行结晶蒸发盐,实现硝盐分离的效果,并且 整个蒸发处理过程实现了零排放。
[0032] 4、本发明的硝蒸发结晶装置和盐蒸发结晶装置分别通过第一蒸汽压缩机和第三 蒸汽压缩机抽取内部蒸发产生的二次蒸汽一方面分别通过第一加热器和第二加热器提高 温度后对硝蒸发结晶装置和盐蒸发结晶装置内的液体进行加热,另一方面通过第一蒸、汽^ 缩机和第二蒸汽压缩机抽取的二次蒸汽同时连接冷却水系统并通过冷冻机和冷却器为冷 冻硝结晶装置提供所需温度,实现高盐废水溶剂充分利用,减少能耗的目的。
附图说明
[0033]图1是本发明的一种高盐废水零排放蒸发结晶盐分质方法的流程图 [0034] 附图标记列表
[0035] 11:增压栗 12:原料进料预热器 13:硝蒸发结晶装置
[0036] 14:硝稠厚器 15:离心分离器 I6:第一蒸汽压缩机
[0037] 17:第一加热器 18:硝母液槽 19:硝母液泵
[0038] 20:冷冻硝结晶装置 21:沉降器 22:冷冻硝离心分离器
[0039] 23:冷冻硝母液槽 24:冷硝母液泵 25:预热器
[0040] 26:真空系统 27:盐蒸发结晶装置 28:循环泵
[0041] 29:第二加热器 30:生蒸汽 31:第二蒸汽压缩机
[0042] 32:稠厚器 33:盐离心分离器 34:硝循环泵
[0043] 35:冷却水系统 36:冷冻机 37:冷却器
[0044] 38:冷冻硝循环泵
具体实施方式
[0045]下面结合附图进行详细说明。本发明提供了一种高盐废水零排放蒸发结晶盐分质 方法。所述方法包括将高浓度盐浓缩液进行分质分离,所述盐浓缩液在进行分质分离前,由 含有复杂成分的废水经过预处理、处理减量化后形成减量浓缩后的高浓度盐浓缩液。
[0046]本发明的高浓缩盐浓缩液在进行分质分离前,包括对污废水进行预处理部分、回 用与减量化部分。所述预处理部分需要的装置包括调节池、提升栗、高密池、增压泵、管式微 滤器、、滤芯过滤器以及污泥池、污泥脱水等设备组成。工业污废水中含有的成分复杂的含 盐废水首先通过调节池进行均质和均量,然后通过提升泵将原水送入高密池,高密池通过 加药装置依次加入石灰或氢氧化钠、碳酸钠、PAC、PAM进行混凝、软化反应。根据本发明的一 种优选实施方式,所述氢氧化钠或石灰的所需量为1.5g/L的20%浓度的溶液;所述碳酸钠 的所需量为3g/L的15 %浓度的溶液;所述PAC的所需量为30mg/L的20 %浓度的溶液;所述 PAM的所需量为3mg/L的0.3 %浓度的溶液。上述加药装置所添加的试剂可根据水质中所含 有的离子浓度进行调整。经过高密池反应产生的沉淀物及絮凝物进入污泥池并通过污泥脱 水后干化处理。经过高密池处理后的产水经增压栗进入管式微滤器,管式微滤器为反渗透 处理的预处理单元,其孔径为1-5微米,能够将在高密池中化学反应产生的沉淀物、混凝胶 体物质进一步去除。再通过滤芯过滤器使前端预处理的废水达到符合后续反渗透进入所需 的SDI指标,降低对后续反渗透膜产生的有机物污染、无机物污堵现象。经过滤芯过滤器过 滤后的上清溶液进入中间水池,从管式微滤器产生的化学沉淀返回高密池通过重力沉降从 底部排入污泥池,经过调整后,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,压滤脱水再进入调节池与原水混合循环处理。
[0047] 本发明的废水处理的回用与减量化部分包括中间水池、增压泵、保安过滤器、中压 反渗透装置、二级反渗透膜、高压反渗透装置、淡水水箱、浓盐水箱、活性炭过滤器、树脂罐、 电驱动离子膜等。经过预处理后的废水去除大部分的硬度及易结垢离子和部分COD后,进入 中间水池收集,利用增压栗提升料液压力后依次使其通过保安过滤器和中压反渗透装置。 根据本发明的一种优选实施方式,中压反渗透装置采用特种浓缩抗污染中压膜元件GTR3-8040F-65,流道宽度为80mil。经过中压反渗透装置后70%原水的产水经过二级反渗透膜后 进入淡水水箱回用,经二级反渗透膜产生的浓离子水再返回预处理后的中间水池进行循环 处理。经过中压反渗透装置后30%原水的反渗透浓液进入中间浓水池,经增压栗提升浓水 压力通过保安过滤器作为高压反渗透装置的进水。根据本发明的一种优选实施方式,高压 反渗透装置采用特种浓缩抗污染高压膜元件GTR4-8040F-80,流道宽度为80mi 1,经过高压 反渗透装置65 %进水的产水经二级反渗透膜进入淡水水箱回用。35 %进水的反渗透浓水进 入中间浓水池收集后通过增压水泵进入活性炭过滤器进行过滤,然后进入树脂罐进行除硬 后进入中间水箱,通过增压水泵经保安过滤器进入一级电驱动离子膜进行深度减量化处 理。经过一级电驱动离子膜约75%的脱盐水返回二级反渗透膜进入淡水水箱回收,经一级 电驱动离子膜后25%的进水进入浓盐水箱收集后经增压水泵进入二级电驱动离子膜进一 步进行深度减量化处理。经二级电驱动离子膜处理后的浓盐水进入浓盐水箱用于后续蒸发 结晶盐分质,淡水再次返回中压反渗透装置后的中压水池循环处理。通过上述减量化部分 处理,约95%以上的优质脱盐水回用。 _
[0048] 图1示出了本发明的高盐废水零排放蒸发结晶分质方法的流程图,如图1所示,经 上述深度浓缩后的剩余约5 %的浓缩盐液自浓盐水箱通过增压栗11进入原料进料预热器 12,经预热后进入硝蒸发结晶装置13将所述高浓度盐浓缩液在负压下由硝蒸发结晶装置13 进行蒸发结晶;所述硝蒸发结晶装置13经硝循环栗34连接第一加热器17对所述硝蒸发结晶 装置13循环加热;所述硝蒸发结晶装置13通过接连真空系统26使所述硝蒸发结晶装置13保 持负压。
[0049] 第一加热器17最初由生蒸汽通过第一加热器17提温后对硝蒸发结晶装置13进行 加热,之后利用第一蒸汽压缩机16进行抽取蒸发后的二次蒸汽压缩通过第一加热器17提高 温度后替代生蒸汽对原料进行持续加热。由所述硝蒸发结晶装置13蒸发产生的二次蒸汽通 过第一蒸汽压缩机16并由第一加热器17提高温度后持续为所述硝蒸发结晶装置13中的盐 浓缩液提供热能。第一加热器17提温后的蒸汽可以用于原料进料预热器内部液体的预热。 硝蒸发结晶装置13在负压状态或微正压下,持续进行水量蒸发浓缩使料液维持在100-115 °C,优选ll〇°C。
[0050] 经蒸发结晶后的固液混合物进入硝稠厚器14进行调整,随后进入离心分离器I5进 行离心分离。分离出的硫酸钠经烘千干燥通过计量包装得到商品硫酸钠。经蒸发结晶后离 心分离产生的硝母液进入硝母液槽18收集,后经硝母液泵I9进入冷冻硝结晶装置20冷冻结 晶。所述硝母液在所述冷冻结晶装置20中进行低温结晶后排放至沉降器21后进行调整,所 述冷冻硝结晶装置20连接冷却器37通过冷硝循环泵38使所述冷冻硝结晶装置20保持低温。 冷冻硝结晶装置20通过冷却器37连接冷冻机36和冷冻循环栗38循环冷却,使其内部母液达 到一 6^^ — 5°C。经冷冻硝结晶装置20冷却结晶后进入沉降器21,通过冷冻硝离心分离器22 离心产生芒硝晶体和冷冻硝母液,所述芒硝晶体再次返回与经所述硝蒸发结晶装置13产生 的硝液热融混合后经离心分离器15分离出硫酸钠;所述冷冻硝母液进入冷冻硝母液槽23经 冷硝母液泵24加入盐蒸发结晶装置27在负压下蒸发结晶得盐。
[0051] 所述冷冻硝母液在冷冻硝母液槽23收集并通过冷冻硝母液泵24首先进入预热器 25进行加热,然后进入盐蒸发结晶装置27在负压下进行蒸发结晶;真空系统26用于维持所 述盐蒸发结晶装置27内保持负压,所述盐蒸发结晶装置27通过循环泵28连接第二加热器29 对所述盐蒸发结晶装置27进行加热,所述盐蒸发结晶装置27产生的二次蒸汽通过第二蒸汽 压缩机31抽取并经第二加热器29提高温度后用于所述预热器25内部液体的加热。
[0052] 所述第二加热器29—方面可用于加热盐蒸发结晶装置内部液体,另一方面可用于 预热器25内部液体的预热。用于盐蒸发结晶装置27加热的最初热量来自生蒸汽30通过第二 加热器29进行加热,之后利用第二蒸汽压缩机31抽取蒸发后的低温二次蒸汽压缩提高温度 替代生蒸汽对原液进行持续加热,盐蒸发产生的二次蒸汽循环加热。盐蒸发结晶装置27在 负压状态下,持续进行水量蒸发浓缩,使内部料液温度维持在5〇_6〇°C。所述经盐蒸发结晶 后的产物通过稠厚器32进入盐离心分离器33再经烘千得到商品盐。
[0053] 另外如图1所示,所述硝蒸发结晶装置13和盐蒸发装置27蒸发产生的二次蒸汽同 时利用第一蒸汽压缩机16和第二蒸汽压缩机31连接冷却水系统35通过冷冻机36为所述第 一蒸汽压缩机16和第二蒸汽压缩机31循环提供冷却水,同时所述冷冻机36连接冷却器37通 过冷硝循环^38保持所述冷冻硝结晶装置20所需温度,实现充分利用高浓度浓缩液中的溶 剂并充分分离溶质的目的。由于在硝蒸发结晶装置13和盐蒸发结晶装置27的蒸发过程中, 二次蒸汽的蒸发会夹带大量的液体,为了防止损失有用的产品或者防止污染冷凝液,需要 在硝蒸发结晶装置13和盐蒸发结晶装置27中加入微量的消泡剂。
[0054]本发明首先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 进行有效的去除,同时通过混凝、吸附的作用去除大部分C0D、有机胶体物质降低浓度,然后 再进入反渗透系统,使反渗透膜表面避免了有机物污染和钙镁结垢的污堵问题。另外本发 明采用管式微滤装置和树脂除硬作为反渗透进水预处理单元,将化学反应生成的沉淀物、 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反渗透进水的SDI指标,降 低了对后续反渗透产生的有机物污染、无机物的污堵,使整个系统处理废水工艺更趋于合 理,保证了系统长期、稳定、可靠运行。
[0055]另外,本发明的中压反渗透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,高压反渗透装置采用流道宽度为80mil (约2.03mm)的特种浓缩抗污染高 压膜元件,高压膜元件具有超大流道的特点,特殊的流道和结构设计,使反渗透膜更不易发 生离子结垢和有机物的污堵。
[0056] 本发明的废水零排放工艺经深度减量化部分对中压反渗透装置和高压反渗透装 置产生的高含盐水进一步减量化处理,利用高效电驱动离子膜对反渗透装置产生的浓水进 一步浓缩,使高盐水从TDS 50000mg/L经一级电驱动离子膜提高到120000mg/L,经过二级电 驱动离子膜提高到200000mg/L以上,与常规多效蒸发减少较低浓度的蒸发水量相比,大幅 度降低蒸发水量,节省能耗,整个工艺流程减量化达到回收水量95%以上,TDS约为 200000mg/L的浓盐液作为蒸发结晶单元原料水。
[0057] 根据本发明的另一个方面,本发明提供了一种用于高盐废水零排放蒸发结晶分质 方法的装置,所述装置包括:增压栗11,所述增压栗11的出口连接原料进料预热器12的第一 进口;所述增压栗11的进口连接浓盐水箱的出口;所述原料进料预热器的出料口连接硝蒸 发结晶装置13的第一进口,所述硝蒸发结晶装置13的第一出口连接第一蒸汽压缩机16的第 一进口,所述硝蒸发结晶装置13的第二出口连接硝循环泵34的进口,硝循环栗34的出口连 接第一加热器17的第一进口;所述第一蒸汽压缩机16的第一出口连接第一加热器17的第二 进口,第一加热器17的第一出口连接原料进料预热器12的第二进口,所述第一加热器17的 第二出口连接硝蒸发结晶装置13的第二进口,所述第一蒸汽压缩机I6的第二出口连接冷却 水系统35的第一进口,硝蒸发结晶装置13的第三出口连接真空系统26的第一进口;硝蒸^ 结晶装置13的第四出口连接硝稠厚器14的进料口;所述硝稠厚器14的出料口连接离心分离 器15的进料口;离心分离器I5的第一出口连接硝母液槽I8的进料口,离心分离器15的第二 出口连接烘干装置的进口;硝母液槽18的出料口连接硝母液泵19的进料口,硝母液泵19的 出料口连接冷冻硝结晶装置2〇的第一进口,所述冷冻硝结晶装置20的第一出口连接沉降器 21的进料口,冷冻硝结晶装置2〇的第二出口连接冷却器37的第—进口,所述冷却器37的第 一出口连接冷冻机36的第一进口,所述冷冻机36的第一出口连接冷却水系统35的第二进 口,所述冷却器37的第二出口连接冷硝循环泵38的进口,所述冷硝循环泵38的出口连接所 述冷冻硝结晶装置2〇的第二进口;所述沉降器21的出料口连接冷冻硝离心分罔器22的进料 口,所述冷冻硝离心分离器22的第一出口连接冷冻硝母淞槽23的进枓口,所还冷你俩方尚 器22的第二出口连接所述硝稠厚器14的进料口;所述冷冻硝母液槽23的出料口连接冷硝母 液泵24的进料口,所述冷硝母液栗24的出料口连接预热器25的第一进口,所述预热器25的 出料口连接盐蒸发结晶装置27的第一进口;所述盐蒸发结晶装置27的第一出口连接循环水 28的进口,所述盐蒸发结晶装置27的第二出口连接稠厚器32的进口,所述盐蒸发结日日装置 27的第三出口连接真空系统26的第二进口;所述循环泵28的出口连接第二加热器29的第一 进口,所述第二加热器29的第一出口连接所述盐蒸发结晶装置27的第二进口,所述第一加 热器29的第二出口连接所述预热器25的第二进口;所述盐蒸发结晶装置27的桌四出口连接 第二蒸汽压缩机31的第一进口,所述第二蒸汽压缩机31的第一出口连接所述第二加热器29 的第二进口,所述第二蒸汽压缩机3丨的第二出口连接所述冷却水系统35的第三进口,所述 冷却水系统35的第一出口连接所述第一蒸汽压缩机16的第二进口,所述冷却水系统35的第 二出口连接所述蒸汽压缩机31的第二进口,所述冷却水系统35的第三出口连接所述冷冻机 36的第二进口,所述冷冻机36的第二出口连接所述冷却器37的第二进口;所述稠厚器32的 出料口连接盐离心分离器33的进料口,所述盐离心分离器33的出料口连接烘干装置的进 □。
[0058] 实施例1
[0059] 取TDS为200000mg/L的经预处理及减量化处理后的高浓度盐浓缩液,通过增压栗 11进入原料进料预热器12进行预热,之后进入硝蒸发结晶装置13。先通入生蒸汽通过第一 加热器17使硝蒸发结晶装置内部料液沸腾后,再利用第一蒸汽压缩机16将蒸发广生的一次 蒸汽抽取并压缩提温后替代生蒸汽对料液进行循环加热,使硝蒸发结晶装置13内部温度保 持在110°C。压缩后的二次蒸汽经过热交换后变成低温冷凝水进入冷却水系统35,进一步通 过冷冻机36和冷却器37降低冷冻硝结晶装置内部温度。硝蒸发结晶装置13内产生的混合物 进入硝稠厚器14进行调整后通过离心分离器15分离出蒸发结晶产生的硫酸钠晶体。离心分 离后的硝母液进入硝母液槽18收集后通过硝母液泵19进入冷冻硝结晶装置20。冷冻硝结晶 装置20利用冷却水系统35通过冷冻机36及冷却器37保持内部温度为一 5°C。冷冻结晶后的 混合物进入冷冻硝离心分离器22离心,离心产生的晶体再次返回进入硝稠厚器14与硝蒸发 结晶产生的物料热融再通过离心分离器分离产生硫酸钠晶体,后经烘干干燥后进行包装。 所得硫酸钠晶体的浓度达到96%。
[0060] 经冷冻硝离心分离器22产生的母液进入冷冻硝母液槽23进行收集后经冷硝母液 泵24进入预热器25进行预热后进入盐蒸发结晶装置27进行低温蒸发。盐蒸发结晶装置27先 通过生蒸汽利用第二加热器29提温后对其加热,然后利用蒸汽压缩机31抽取盐蒸发产生的 二次蒸汽压缩提温后使盐蒸发结晶装置27内部温度保持在50°C。压缩后的二次蒸汽经过热 交换后变成低温冷凝水进入冷却水系统35,进一步通过冷冻机36和冷却器37降低冷冻硝结 晶装置内部温度。真空系统用来保持盐蒸发结晶装置27和硝蒸发结晶装置13内部负压的状 态或不采用真空系统保持微正压状态。
[0061]经验蒸发结晶产生的混合物料进入稠厚器32调整后进入盐离心分离器33进行离 心分离,将分离产生的氯化钠晶体烘干干燥进行包装。所得氯化钠浓度达98%。
[0062] 实施例2
[0063]取TDS为210000mg/L的经预处理及减量化处理后的高浓度盐浓缩液,通过增压泵 11进入原料进料预热器12进行预热,之后进入硝蒸发结晶装置13。先通入生蒸汽通过第一 加热器17使硝蒸发结晶装置内部料液沸腾后,再利用第一蒸汽压缩机16将蒸发产生的二次 蒸汽抽取并压缩提温后替代生蒸汽对料液进行循环加热,使硝蒸发结晶装置13内部温度保 持在100°C。压缩后的二次蒸汽经过热交换后变成低温冷凝水进入冷却水系统35,进一步通 过冷冻机3e和冷却器37降低冷冻硝结晶装置内部温度。硝蒸发结晶装置13内产生的混合物 进入硝稠厚器14进行调整后通过离心分离器I5分离出蒸发结晶产生的硫酸钠晶体。离心分 离后的硝母液进入硝母液槽18收集后通过硝母液栗IQ进入冷冻硝结晶装置20。冷冻硝结晶 装置20利用冷却水系统35通过冷冻机36及冷却器37保持内部温度为一 6-C。冷冻结晶后的 混合物进入冷冻硝离心分离器22离心,离心产生的晶体再次返回进入硝稠厚器14与硝蒸发 结晶产生的混合物热融再通过离心分离器分离产生硫酸钠晶体,后经供干干燥后进行包 装。所得硫酸钠晶体的浓度达到97%。
[0064] 经冷冻硝离心分离器22产生的母液进入冷冻硝母液槽M进行收集后经冷硝母液 栗24进入预热器25进行预热后进入盐蒸发结晶装置27进行低温蒸发。盐蒸发结晶装置27先 通过生蒸汽利用第二加热器29提温后对其加热,然后利用蒸汽压缩机31抽取盐蒸发产生的 二次蒸汽压缩提温后使盐蒸发结晶装置27内部保持在60°C。压缩后的二次蒸汽经过热交换 后变成低温冷凝水进入冷却水系统35,进一步通过冷冻机36和冷却器37降低冷冻硝结晶装 置内部温度。真空系统用来保持盐蒸发结晶装置27和硝蒸发结晶装置13内部负压的状态或 不采用真空系统保持微正压状态。
[0065]经验蒸发结晶产生的混合物料进入稠厚器32调整后进入盐离心分离器33进行离 心分离,将分离产生的氯化钠晶体烘干千燥进行包装。所得氯化钠浓度达99%。
[0066] 实施例3
[0067]取TDS为220000mg/L的经预处理及减量化处理后的高浓度盐浓缩液,通过增压栗 11进入原料进料预热器12进行预热,之后进入硝蒸发结晶装置13。先通入生蒸汽通过第一 加热器17使硝蒸发结晶装置内部料液沸腾后,再利用第一蒸汽压缩机16将蒸发产生的二次 蒸汽抽取并压缩提温后替代生蒸汽对料液进行循环加热,使硝蒸发结晶装置13内部温度保 持在115°C。压缩后的二次蒸汽经过热交换后变成低温冷凝水进入冷却水系统35,进一步通 过冷冻机36和冷却器37降低冷冻硝结晶装置内部温度。硝蒸发结晶装置13内产生的物料进 入硝稠厚器14进行调整后通过离心分离器15分离出蒸发结晶产生的硫酸钠晶体。离心分离 后的硝母液进入硝母液槽I8收集后通过硝母液泵I9进入冷冻硝结晶装置20。冷冻硝结晶装 置20利用冷却水系统35通过冷冻机36及冷却器37保持内部温度为一 5°C。冷冻结晶后的混 合物进入冷冻硝离心分离器22离心,离心产生的晶体再次返回进入硝稠厚器14与硝蒸发结 晶产生的物料热融再通过离心分离器分离产生硫酸钠晶体,后经烘干干燥后进行包装。所 得硫酸钠晶体的浓度达到明%。
[0068]经冷冻硝离心分离器22产生的母液进入冷冻硝母液槽23进行收集后经冷硝母液 泵24进入预热器25进行预热后进入盐蒸发结晶装置27进行低温蒸发。盐蒸发结晶装置27先 通过生蒸汽利用第二加热器29提温后对其加热,然后利用第二蒸汽压缩机31抽取盐蒸发产 生的二次蒸汽压缩提温后使盐蒸发结晶装置27内部温度保持在55°C。压缩后的二次蒸汽经 过热交换后变成低温冷凝水进入冷却水系统35,进一步通过冷冻机36和冷却器37降低冷冻 硝结晶装置内部温度。真空系统用来保持盐蒸发结晶装置27和硝蒸发结晶装置13内部负压 的状态或不采用真空系统保持微正压状态。
[0069] 经验蒸发结晶产生的混合物料进入稠厚器32调整后进入盐离心分离器33进行离 心分离,将分离产生的氯化钠晶体烘干干燥进行包装。所得氯化钠浓度达98.5%。
[0070]本发明的零排工艺蒸发结晶,经过前述两级减量化过程,形成的高浓度盐液进入 蒸发结晶的预热器、硝蒸发结晶装置,在负压状态下进行蒸发结晶。利用生蒸汽提供初步热 量加热盐液至沸腾,然后利用蒸发产生的低温二次乏汽通过蒸汽压缩机进行压缩提高乏汽 的温度,实现持续为硝罐盐液提供热能。利用水盐体系Na+/Cl_,SO/—-似0相图,进行硫酸钠 和氯化钠的结晶分离,根据相图采用低温冷冻方式进一步分离出芒硝,把芒硝回溶到结晶 罐与待分离的料液共同进行热融析出硫酸钠,最终达到对硫酸钠和氯化钠进行分质分离。 同时利用蒸汽压缩机抽取蒸发产生的二次蒸汽用于循环冷却水系统,利用冷冻机和冷却器 为冷冻硝结晶装置内保持低温。实现充分利用溶剂和分离溶质的效果。本发明的分质盐分 离硫酸钠浓度可达96%以上,氯化钠浓度⑽%以上,最终混盐占总盐量5%以下,产水全部 回收利用,无废水排放,达到废水零排放的效果。
[0071]需要注意的是,上述具体实施例是示例性的,本领域技术人员可以在本发明公开 内容的启发下想出各种解决方案,而这些解决方案也都属于本发明的公开范围并落入本发 明的保护范围之内。本领域技术人员应该明白,本发明说明书及其附图均为说明性而并非 构成对权利要求的限制。本发明的保护范围由权利要求及其等同物限定。
Claims (10)
1. 一种盐分质系统,其用于对高盐废水进行蒸发结晶,其特征在于,所述系统包括硝蒸 发结晶装置(13)、冷冻硝结晶装置(20)和盐蒸发结晶装置(27),其中,所述硝蒸发结晶装置 (13)和所述盐蒸发结晶装置(27)在分别利用第一蒸汽压缩机(16)和第二蒸汽压缩机(31) 抽取并压缩二次蒸汽的条件下参照冷冻硝结晶所需温度通过所述第一蒸汽压缩机(16)和 所述第二蒸汽压缩机(31)连接冷却水系统(35)并利用冷却器(37)和/或冷冻机(36)保持所 述冷冻硝结晶装置(20)内部所需温度。
2. 根据权利要求1所述的盐分质系统,其特征在于,依次通过所述硝蒸发结晶装置 (13)、所述冷冻硝结晶装置(20)和所述盐蒸发结晶装置(27)使得经预处理及深度浓缩后的 高浓度盐浓缩液按照硫酸钠、氯化钠的分离顺序进行分质,其中, 所述硝蒸发结晶装置(13)用于使得所述高浓度盐浓缩液在负压或微正压下进行蒸发 结晶; 所述冷冻硝结晶装置(20)用于使得蒸发结晶产生的硝母液被冷冻结晶,经所述冷冻硝 结晶装置(20)产生的混合物通过冷冻硝离心分离器(22)离心,离心产生的晶体再次返回与 经所述硝蒸发结晶装置(13)产生的硝液热融混合后再经离心分离器(15)分离出硫酸钠晶 体。
3. 根据权利要求2所述的盐分质系统,其特征在于,所述硝蒸发结晶装置(13)和所述盐 蒸发结晶装置(27)蒸发产生的二次蒸汽分别通过所述第一蒸汽压缩机(16)和所述第二蒸 汽压缩机(31)连接冷却水系统(35)并通过冷冻机(36)为所述第一蒸汽压缩机(16)和所述 第二蒸汽压缩机(31)提供循环冷却水,并且所述冷冻机(36)连接冷却器(37)并通过冷硝循 环栗(38)保持所述冷冻硝结晶装置(20)维持在一6^^ — 5°C。
4. 如权利要求1-3之一所述的盐分质系统,其特征在于, 经所述冷冻硝离心分离器(22)离心产生的冷冻硝母液经冷硝母液泵(24)加入所述盐 蒸发结晶装置(27)并在负压下蒸发结晶得盐; 由所述硝蒸发结晶装置(13)和所述盐蒸发结晶装置(27)蒸发产生的二次蒸汽分别通 过第一蒸汽压缩机(16)和第二蒸汽压缩机(31)抽取并分别由第一加热器(17)和第二加热 器(29)提高温度后持续为所述硝蒸发结晶装置(13)和所述盐蒸发结晶装置(27)中的浓缩 液提供热能。 所述高浓度盐浓缩液在进行分质前,由含有复杂成分的废水依次经过预处理部分、回 用与减量化部分后形成减量浓缩后的高浓度盐浓缩液。
5. 如权利要求2或3所述的盐分质系统,其特征在于,所述高浓度盐浓缩液通过增压栗 (11)进入原料进料预热器(12)预热后经所述硝蒸发结晶装置(13)进行负压或微正压蒸发 结晶,所述硝蒸发结晶装置(13)经硝循环泵(34)连接所述第一加热器(17)对所述硝蒸发结 晶装置(13)循环加热;所述硝蒸发结晶装置(13)通过接连真空系统(26)使所述硝蒸发结晶 装置(13)保持负压。
6. 如权利要求1-3之一所述的盐分质系统,其特征在于,所述硝蒸发结晶装置(1¾在负 压或微正压状态下,持续进行水分蒸发浓缩,所述硝蒸发结晶装置(13)内高盐浓缩液的温 度维持在100〜115°C。
7. 如权利要求1-3之一所述的盐分质系统,其特征在于,所述高浓度盐浓缩液经所述硝 蒸发结晶装置(13)蒸发结晶后进入硝稠厚器(14)进行调整后进入离心分离器(15),经离心 后的硫酸钠晶体经烘干设备干燥后,进行计量包装得到商品硫酸钠。
8.如权利要求2-3之一所述的盐分质系统,其特征在于,所述离心分离器(15)中产生的 硝母液进入硝母液槽(18),并经硝母液泵(19)进入所述冷冻硝结晶装置(20)进行降温结 晶。
9. 如权利要求2-3之一所述的盐分质系统,其特征在于,所述硝母液在所述冷冻硝结晶 装置(20)中进行结晶后排放至沉降器(21)后进行调整,所述冷冻硝结晶装置(20)连接冷却 器(37)并通过冷硝循环泵(38)使所述冷冻硝结晶装置(20)保持在一6〜一5°C ; 所述冷冻硝母液通过冷冻硝母液泵(24)进入预热器(25)进行加热,然后进入所述盐蒸 发结晶装置(27)并在负压下进行蒸发结晶; 所述盐蒸发结晶装置(27)通过循环泵(28)连接第二加热器(29)对所述盐蒸发结晶装 置(27)进行加热,所述盐蒸发结晶装置(27)产生的二次蒸汽通过所述第二蒸汽压缩机(31) 抽取并经第二加热器(29)提高温度后用于所述预热器(25)内部液体的加热; 经盐蒸发结晶后的产物通过稠厚器(32)进入盐离心分离器(33)分离后,再将晶体经烘 干得到商品盐。
10. —种高盐废水零排放蒸发结晶盐分质方法,其特征在于, 依次通过硝蒸发结晶装置(13)、冷冻硝结晶装置(20)和盐蒸发结晶装置(27)使得经预 处理及深度浓缩后的高浓度盐浓缩液按照硫酸钠、氯化钠的分离顺序进行分质,其中, 所述硝蒸发结晶装置(13)用于使得所述高浓度盐浓缩液在负压或微正压下进行蒸发 结晶; 所述冷冻硝结晶装置(20)用于使得蒸发结晶产生的硝母液被冷冻结晶,经所述冷冻硝 结晶装置(20)产生的混合物通过冷冻硝离心分离器(22)离心,离心产生的晶体再次返回与 经所述硝蒸发结晶装置(13)产生的硝液热融混合后再经离心分离器(15)分离出硫酸钠晶 体; 经所述冷冻硝离心分离器(22)离心产生的冷冻硝母液经冷硝母液泵(24)加入所述盐 蒸发结晶装置(27)并在负压下蒸发结晶得盐; 由所述硝蒸发结晶装置(13)和所述盐蒸发结晶装置(27)蒸发产生的二次蒸汽分别通 过第一蒸汽压缩机(16)和第二蒸汽压缩机(31)抽取并分别由第一加热器(1乃和第二加热 器(29)提高温度后持续为所述硝蒸发结晶装置(I3)和所述盐蒸发结晶装置(27)中的浓缩 液提供热能。
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