CN107555449A - 一种反渗透浓缩并且回收利用氯化铵溶液的方法 - Google Patents
一种反渗透浓缩并且回收利用氯化铵溶液的方法 Download PDFInfo
- Publication number
- CN107555449A CN107555449A CN201710943001.3A CN201710943001A CN107555449A CN 107555449 A CN107555449 A CN 107555449A CN 201710943001 A CN201710943001 A CN 201710943001A CN 107555449 A CN107555449 A CN 107555449A
- Authority
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- China
- Prior art keywords
- ammonium chloride
- chloride solution
- stoste
- concentration
- reverse osmosis
- Prior art date
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- 235000019270 ammonium chloride Nutrition 0.000 title claims abstract description 224
- QDHHCQZDFGDHMP-UHFFFAOYSA-N monochloramine Chemical compound 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ClN QDHHCQZDFGDHMP-UHFFFAOYSA-N 0.000 title claims abstract description 224
- 238000001223 reverse osmosis Methods 0.000 title claims abstract description 52
- 238000004064 recycling Methods 0.000 title claims description 8
- 239000004259 Ammonium chloride Substances 0.000 title abstract 16
- 230000000149 penetrating Effects 0.000 claims abstract description 33
- 238000001816 cooling Methods 0.000 claims abstract description 21
- 239000008235 industrial waters Substances 0.000 claims abstract description 17
- 239000012141 concentrates Substances 0.000 claims abstract description 12
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances 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[NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 claims description 208
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- 239000011550 stock solution Substances 0.000 description 3
- AXCZMVOFGPJBDE-UHFFFAOYSA-L Calcium hydroxide Chemical compound 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[OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O ammonium Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,PD94bWwgdmVyc2lvbj0nMS4wJyBlbmNvZGluZz0naXNvLTg4NTktMSc/Pgo8c3ZnIHZlcnNpb249JzEuMScgYmFzZVByb2ZpbGU9J2Z1bGwnCiAgICAgICAgICAgICAgeG1sbnM9J2h0dHA6Ly93d3cudzMub3JnLzIwMDAvc3ZnJwogICAgICAgICAgICAgICAgICAgICAgeG1sbnM6cmRraXQ9J2h0dHA6Ly93d3cucmRraXQub3JnL3htbCcKICAgICAgICAgICAgICAgICAgICAgIHhtbG5zOnhsaW5rPSdodHRwOi8vd3d3LnczLm9yZy8xOTk5L3hsaW5rJwogICAgICAgICAgICAgICAgICB4bWw6c3BhY2U9J3ByZXNlcnZlJwp3aWR0aD0nODVweCcgaGVpZ2h0PSc4NXB4JyB2aWV3Qm94PScwIDAgODUgODUnPgo8IS0tIEVORCBPRiBIRUFERVIgLS0+CjxyZWN0IHN0eWxlPSdvcGFjaXR5OjEuMDtmaWxsOiNGRkZGRkY7c3Ryb2tlOm5vbmUnIHdpZHRoPSc4NScgaGVpZ2h0PSc4NScgeD0nMCcgeT0nMCc+IDwvcmVjdD4KPHRleHQgeD0nMzUuMDQ1NScgeT0nNTMuNTkwOScgY2xhc3M9J2F0b20tMCcgc3R5bGU9J2ZvbnQtc2l6ZToyM3B4O2ZvbnQtc3R5bGU6bm9ybWFsO2ZvbnQtd2VpZ2h0Om5vcm1hbDtmaWxsLW9wYWNpdHk6MTtzdHJva2U6bm9uZTtmb250LWZhbWlseTpzYW5zLXNlcmlmO3RleHQtYW5jaG9yOnN0YXJ0O2ZpbGw6IzQyODRGNCcgPk48L3RleHQ+Cjx0ZXh0IHg9JzUxLjA0MDknIHk9JzUzLjU5MDknIGNsYXNzPSdhdG9tLTAnIHN0eWxlPSdmb250LXNpemU6MjNweDtmb250LXN0eWxlOm5vcm1hbDtmb250LXdlaWdodDpub3JtYWw7ZmlsbC1vcGFjaXR5OjE7c3Ryb2tlOm5vbmU7Zm9udC1mYW1pbHk6c2Fucy1zZXJpZjt0ZXh0LWFuY2hvcjpzdGFydDtmaWxsOiM0Mjg0RjQnID5IPC90ZXh0Pgo8dGV4dCB4PSc2Ny4wMzY0JyB5PSc2Mi44NjM2JyBjbGFzcz0nYXRvbS0wJyBzdHlsZT0nZm9udC1zaXplOjE1cHg7Zm9udC1zdHlsZTpub3JtYWw7Zm9udC13ZWlnaHQ6bm9ybWFsO2ZpbGwtb3BhY2l0eToxO3N0cm9rZTpub25lO2ZvbnQtZmFtaWx5OnNhbnMtc2VyaWY7dGV4dC1hbmNob3I6c3RhcnQ7ZmlsbDojNDI4NEY0JyA+NDwvdGV4dD4KPHRleHQgeD0nNjcuMDM2NCcgeT0nNDQuMzE4MicgY2xhc3M9J2F0b20tMCcgc3R5bGU9J2ZvbnQtc2l6ZToxNXB4O2ZvbnQtc3R5bGU6bm9ybWFsO2ZvbnQtd2VpZ2h0Om5vcm1hbDtmaWxsLW9wYWNpdHk6MTtzdHJva2U6bm9uZTtmb250LWZhbWlseTpzYW5zLXNlcmlmO3RleHQtYW5jaG9yOnN0YXJ0O2ZpbGw6IzQyODRGNCcgPis8L3RleHQ+Cjwvc3ZnPgo= [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 2
- 150000003863 ammonium salts Chemical class 0.000 description 2
- 239000000920 calcium hydroxide Substances 0.000 description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 2
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Inorganic materials 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Abstract
本发明公开了一种反渗透浓缩并且回收利用氯化铵溶液的方法,包括以下步骤:冷却氯化铵原液;过滤氯化铵原液;将氯化铵原液一次反渗透浓缩得到浓缩氯化铵溶液和渗透液;冷却浓缩氯化铵溶液;将渗透液二次反渗透脱盐得到氯化铵原液和第一脱盐水;第一脱盐水用于冷却氯化铵原液得到第二脱盐水;浓缩氯化铵溶液通过能量回收装置给一次反渗透浓缩供给能量;第二脱盐水被浓缩氯化铵溶液冷却得到工业用水。本发明浓缩并且回收利用氯化铵溶液的方法生产的氯化铵溶液浓度高;同时本发明可回收浓缩氯化铵溶液的能量对浓缩过程供能并且浓缩氯化铵溶液后得到的脱盐水也可回收冷却氯化铵原液,降低了生产成本,操作工艺简便,便于工业生产。
Description
一种反渗透浓缩并且回收利用氯化铵溶液的方法
技术领域
[0001 ]本发明涉及浓缩氯化铵溶液的方法,具体涉及一种利用反渗透技术浓缩并且回收 利用氯化铵溶液的方法。
背景技术
[0002]工业生产,例如生产硝酸钾的过程中,会产生废液氯化铵溶液。这种氯化铵溶液经 过纯化处理后,溶液中的氯化铵浓度增加。为了回收氯化铵,这种氯化铵溶液需要进一步盐 田晾晒,得到氯化铵颗粒。目前,氯化铵溶液处理有两套生产工艺。第一套工艺将氯化铵溶 液排至盐田晾晒,自然蒸发结晶,待水份蒸发完毕后采收包装销售,但氯化铵的成品价格很 低,经济效益很差。第二套工艺氯化铵溶液排至盐田晾晒,自然蒸发浓缩至一定浓度后,输 送至氯化铵车间加入氢氧化钙(Ca (0H) 2),生成氨气(NH3) <3 2NH4C1+Ca (OH) 2 = CaCl2+2NH3T+ 別2〇。将氨气(Mfe)回收制成液氨,供盐湖三期或硝酸硝铵车间使用。无论上述那种生产工艺 都需要高浓度氯化铵溶液进入盐田,以缩短盐田晾晒周期。若将交换工序产生的高浓度氯 化铵溶液和氯化铵原液直接混合排至盐田晾晒,氯化铵的晾晒周期较长,需要盐田数量多, 且浪费了大量的水。同时,本装置生产所用脱盐水基本为外供,时常出现脱盐水供应不足, 制约生产。
[0003] 综上所述,现有技术中的氯化铵溶液处理存在氯化铵成品质量差,氯化铵浓度低, 生产过程耗能多,用水量大的问题。
发明内容
[0004] 本发明通过回收浓缩后氯化铵溶液的能量向反渗透功能并且回收反渗透过程生 成的脱盐水进行冷却同时用作后续的工业用水,解决了现有技术中浓缩氯化铵溶液耗能 大、用水量多的问题。
[0005] 为了解决上述技术问题,本发明提供了一种反渗透浓缩并且回收利用氯化铵溶液 的方法,包括以下步骤:冷却氯化铵原液;过滤氯化铵原液;将氯化铵原液一次反渗透浓缩 得到浓缩氯化铵溶液和渗透液;冷却第二脱盐水;将渗透液二次反渗透脱盐得到氯化铵原 液和第一脱盐水;第一脱盐水用于冷却氯化铵原液得到第二脱盐水;浓缩氯化铵溶液通过 能量回收装置给一次反渗透浓缩供给能量;第二脱盐水冷却浓缩氯化铵溶液得到工业用 水。
[0006] 进一步地,冷却后氯化铵原液的温度为15-25°c。
[0007] 进一步地,第一脱盐水在氯化铵原液中的含量为58 % -70 %。
[0008] 进一步地,第二脱盐水的温度为60_65°C。
[0009] 进一步地,工业用水的温度为50-55 °C。
[0010]进一步地,一次反渗透浓缩和二次反渗透脱盐可采用多段渗透膜。
[0011] 进一步地,浓缩氯化铵溶液通过能量回收装置对进入渗透膜的溶液进行增压。
[0012] 和现有技术相比,本发明反渗透浓缩并且回收利用氯化铵溶液的方法具有下述优 占.
[0013] —、通过使用两次反渗透装置处理浓缩氯化铵原液,提高了氯化铵原液浓度,从而 提高了打入盐田氯化铵溶液的浓度,缩短了氯化铵溶液的晾晒周期;
[0014]二、回收了氯化铵原液中的脱盐水用于生产,减少了外供脱盐水量,降低了生产成 本;
[0015] 三、本发明的反渗透工艺成熟、操作过程简、各步骤和参数均易控制,所用设备制 稳定性强、自动化程度高、安全可靠。
附图说明
[0016] 图1是本发明反渗透浓缩并且回收利用氯化铵溶液的方法的流程图。
具体实施方式
[0017] 下面结合附图,对本发明反渗透浓缩并且回收利用氯化铵溶液的方法进行说明。
[0018] 参见图1,图解了本发明反渗透浓缩并且回收利用氯化铵溶液的方法的流程图。本 发明反渗透浓缩并且回收利用氯化铵溶液的方法包括:S1:第一脱盐水冷却氯化铵原液,得 到第二脱盐水;S2:过滤氯化铵溶液;S3:将氯化铵溶液一次反渗透浓缩得到浓缩氯化铵溶 液和渗透液;S4:第二脱盐水被浓缩氯化铵溶液冷却,得到产品氯化铵溶液和工业用水;S5: 将渗透液二次反渗透得到氯化铵溶液和第一脱盐水。
[0019] 需要说明的是,由于利用反渗透技术浓缩氯化铵溶液时,反渗透装置的膜温度不 能太高,所以进入反渗透设备前氯化铵溶液温度需要冷却。本发明反渗透浓缩并且回收利 用氯化铵溶液的方法利用反渗透过程中产生的脱盐水冷却氯化铵溶液,实现脱盐水的循环 利用,得到温度适宜的工业用水。也就是说,冷却是利用整个反渗透过程完成后生成的脱盐 水进行。
[0020] 需要说明的是,在本发明进行浓缩氯化铵溶液之前,需要收集低浓度氯化铵溶液, 这种氯化铵原液由交换工序产生,称为氯化铵原液,收集在氯化铵储罐。
[0021] S1:第一脱盐水冷却氯化铵原液,得到第二脱盐水。利用第一脱盐水对氯化铵原液 降温,同时回收氯化铵原液的热能。用泵将氯化铵泵入换热系统,依次进入前置换热器、热 泵机组与第一脱盐水换热,氯化铵原液的温度降至15-25°c,得到氯化铵原液同时回收热量 给第一脱盐水加热。氯化铵原液进入一次反渗透装置。
[0022] S2:过滤氯化铵溶液。氯化铵原液需要先进行过滤,作为本发明的一个实施例,先 通过自清洗装置过滤氯化铵原液中较大粒径(例如>50um)的杂质,再进入保安过滤器过滤 氯化铵原液中较小粒径(例如>5um)的杂质。
[0023] S3:将氯化铵溶液一次反渗透浓缩得到浓缩氯化铵溶液和渗透液。经两次过滤后 的氯化铵原液由一次高压泵打入一次反渗透本体装置,一次反渗透本体装置利用反渗透膜 (例如海水淡化膜)的特性浓缩氯化铵原液,将大部分水分离出来得到渗透液。
[0024]在本发明中,一次反渗透过程具有多个阶段的渗透膜,对氯化铵原液进行反渗透 浓缩。所属领域的技术人员可知的是,经过渗透膜之后,溶液的渗透压会逐渐减小,此时渗 透的效率会逐渐降低。一般地,本领域会利用额外的供能设备增加渗透设备中溶液的渗透 压。本发明反渗透浓缩并且回收利用氯化铵溶液的方法在一段浓缩氯化铵溶液进入二段时 采用了能量回收装置,将渗透后浓缩得到的浓缩氯化铵溶液的高压转化为能量,对接下来 的多阶段渗透过程的溶液间断增压,同时使反渗透得到的浓缩氯化铵溶液解压便于回收。 [0025] S4:第二脱盐水被浓缩氯化铵溶液冷却,得到产品氯化铵溶液和工业用水;浓缩后 的高浓度氯化铵溶液,经后置换热器与第二脱盐水换热后去往氯化铵溶液储槽再由泵输送 至盐田晾晒。从氯化铵原液分离出渗透液进入缓冲水箱。渗透液中含有少量的氯化铵,还不 能满足生产工艺用水要求。第一脱盐水由泵依次泵入前置换热器、热泵机组与氯化铵原液 进行换热,将第一脱盐水温度升至60-65°C (例如60°C、61°C、62°C、63°C、64°C、65°C),得到 第二脱盐水,再经后置换热器与一次反渗透浓缩后的氯化铵溶液换热,温度降低至50-55°C (例如5〇°(:、51°(:、52°(:、53°(:、54°(:、55°(:),存储在脱盐水储罐供生产使用。
[0026] S5:将渗透液二次反渗透得到氯化铵原液和第一脱盐水。缓冲水箱的渗透液由二 次高压栗打入二次反渗透本体装置,二次反渗透本体装置利用反渗透膜(低脱盐膜)的特性 脱去渗透液中的氯化铵,制得第一脱盐水,回收至脱盐水缓冲罐。浓缩氯化铵溶液去往氯化 铵原液储罐,与氯化铵原液混合进入浓缩过程。
[0027]具体实施例;
[0028] 实施例1
[0029] S1:第一脱盐水冷却氯化铵原液,得到第二脱盐水。收集氯化铵原液,在交换工序 产生的氯化铵原液收集在氯化铵储罐,氯化铵平均浓度13g/l、温度50°C。对氯化铵原液降 温,同时回收氯化铵原液的热能。用栗将氯化铵打入换热系统,依次进入前置换热器、热栗 机组与第一脱盐水换热,氯化铵原液的温度降至15-25°C,得到氯化铵原液,同时回收热量 给第一脱盐水加热,第一脱盐水温度升至6〇-65°C,得到第二脱盐水。
[0030] S2:过滤氯化铵溶液。氯化铵原液先通过自清洗装置过滤氯化铵原液中较大粒径 (例如>50um)的杂质,再进入保安过滤器过滤氯化铵原液中较小粒径(例如>5um)的杂质。 [0031] S3:将氯化铵溶液一次反渗透浓缩得到浓缩氯化铵溶液和渗透液。经两次过滤后 的氯化铵原液由一次高压泵打入一次反渗透本体装置,进液压力为3-3.2Mpa,一次反渗透 本体装置将第二低浓度氯化铵原液浓缩为高浓度氯化铵溶液,经后置换热器与第二脱盐水 换热后去往氯化铵溶液储槽,再由泵输送至盐田晾晒。从氯化铵原液分离出的渗透液(约 72%)进入缓冲水箱。渗透液中含有少量的氯化铵,还不能满足生产用水要求。
[0032] S4:第二脱盐水被浓缩氯化铵溶液冷却,得到产品氯化铵溶液和工业用水。第一脱 盐水由栗依次泵入前置换热器、热荥机组与氯化铵原液进行换热,将第一脱盐水温度升至 60-65 °C,得到第二脱盐水,再经后置换热器与一次反渗透浓缩后的氯化铵溶液换热后,温 度降低至50-55°C (满足生产用水温度),存储在脱盐水储罐供生产使用。回收低浓度氯化铵 原液中67%的水,用于生产。浓缩后的氯化铵溶液浓度为4味/1。
[0033] S5:将渗透液二次反渗透得到氯化铵溶液和第一脱盐水。缓冲水箱的渗透液由二 次高压杲打入二次反渗透本体装置,进液压力为IMpa。二次反渗透本体装置利用反渗透膜 (低脱盐膜)将渗透液中氯化铵脱去,得到第一脱盐水温度为15-25°C,回收率约为93%,第 一脱盐水回收至脱盐水缓冲罐。浓缩氯化铵溶液去往氯化铵原液储罐,与氯化铵原液混合 进入浓缩过程。
[0034] 实施例2
[0035] S1:第一脱盐水冷却氯化铵原液,得到第二脱盐水。收集氯化铵原液,在交换工序 产生的氯化铵原液收集在氯化铵储罐,氯化铵平均浓度13g/l、温度45°C。对氯化铵原液降 温,同时回收氯化铵原液的热能。用泵将氯化铵打入换热系统,依次进入前置换热器、热栗 机组与第一脱盐水换热,氯化铵原液的温度降至15-25°C,得到氯化铵原液,同时回收热量 给第一脱盐水加热,第一脱盐水温度升至60-65°C,得到第二脱盐水。
[0036] S2:过滤氯化铵溶液。氯化铵原液先通过自清洗装置过滤氯化铵原液中较大粒径 (例如>50um)的杂质,再进入保安过滤器过滤氯化铵原液中较小粒径(例如>5um)的杂质。 [0037] S3:将氯化铵溶液一次反渗透浓缩得到浓缩氯化铵溶液和渗透液。经两次过滤后 的氯化铵原液由一次高压泵打入一次反渗透本体装置,进液压力为3.3-3.5Mpa,一次反渗 透本体装置将第二低浓度氯化铵原液浓缩为高浓度氯化铵溶液,经后置换热器与第二脱盐 水换热后去往氯化铵溶液储槽,再由泵输送至盐田晾晒。从氯化铵原液分离出的渗透液(约 68%)进入缓冲水箱。渗透液中含有少量的氯化铵,还不能满足生产用水要求。
[0038] S4:第二脱盐水被浓缩氯化铵溶液冷却,得到产品氯化铵溶液和工业用水。第一脱 盐水由泵依次泵入前置换热器、热泵机组与氯化铵原液进行换热,将第一脱盐水温度升至 60-65°C,得到第二脱盐水,再经后置换热器与一次反渗透浓缩后的氯化铵溶液换热后,温 度降低至50-55°C (满足生产用水温度),存储在脱盐水储罐供生产使用。回收低浓度氯化铵 原液中62%的水,用于生产。浓缩后的氯化铵溶液浓度为46g/l。
[0039] S5:将渗透液二次反渗透得到氯化铵溶液和第一脱盐水。缓冲水箱的渗透液由二 次高压泵打入二次反渗透本体装置,进液压力为IMpa。二次反渗透本体装置利用反渗透膜 (低脱盐膜)将渗透液中氯化铵脱去,得到第一脱盐水温度为15-25°C,回收率约为92%,第 一脱盐水回收至脱盐水缓冲罐。浓缩氯化铵溶液去往氯化铵原液储罐,与氯化铵原液混合 进入浓缩过程。
[0040] 实施例3
[0041] S1:第一脱盐水冷却氯化铵原液,得到第二脱盐水。收集氯化铵原液,在交换工序 产生的氯化铵原液收集在氯化铵储罐,氯化铵平均浓度15g/l、温度52°C。对氯化铵原液降 温,同时回收氯化铵原液的热能。用泵将氯化铵打入换热系统,依次进入前置换热器、热栗 机组与第一脱盐水换热,氯化铵原液的温度降至15-25 °C,得到氯化铵原液,同时回收热量 给第一脱盐水加热,第一脱盐水温度升至6〇_65°C,得到第二脱盐水。
[0042] S2:过滤氯化铵溶液。氯化铵原液先通过自清洗装置过滤氯化铵原液中较大粒径 (例如>50um)的杂质,再进入保安过滤器过滤氯化铵原液中较小粒径(例如>5um)的杂质。
[0043] S3:将氯化铵溶液一次反渗透浓缩得到浓缩氯化铵溶液和渗透液。经两次过滤后 的氯化铵原液由一次高压泵打入一次反渗透本体装置,进液压力为3.3-3 • 5Mpa,一次反渗 透本体装置将第二低浓度氯化铵原液浓缩为高浓度氯化铵溶液,经后置换热器与第二脱盐 水换热后去往氯化按溶液储槽,再由栗输送至盐田晾晒。从氯化按原液分离出的渗透液(约 70%)进入缓冲水箱。渗透液中含有少量的氯化铵,还不能满足生产用水要求。
[0044] S4:第二脱盐水被浓缩氯化铵溶液冷却,得到产品氯化铵溶液和工业用水。第一脱 盐水由栗依次泵入前置换热器、热泵机组与氯化铵原液进行换热,将第一脱盐水温度升至 60-65 °C,得到第二脱盐水,再经后置换热器与一次反渗透浓缩后的氯化铵溶液换热后,温 度降低至50-55°C (满足生产用水温度),存储在脱盐水储罐供生产使用。回收低浓度氯化铵 原液中64.4 %的水,用于生产。浓缩后的氯化铵溶液浓度为47g/l。
[0045] S5:将渗透液二次反渗透得到氯化铵溶液和第一脱盐水。缓冲水箱的渗透液由二 次咼压泵打入一次反渗透本体装置,进液压力为IMpa。二次反渗透本体装置利用反渗透膜 (低脱盐膜)将渗透液中氯化铵脱去,得到第一脱盐水温度为15-25°C,回收率约为92%,第 一脱盐水回收至脱盐水缓冲罐。浓缩氯化铵溶液去往氯化铵原液储罐,与氯化铵原液混合 进入浓缩过程。
[0046] 上述说明示出并描述了本申请的若干优选实施例,但如前所述,应当理解本申请 并非局限于本文所披露的形式,不应看作是对其他实施例的排除,而可用于各种其他组合、 修改和环境,并能够在本文所述发明构想范围内,通过上述教导或相关领域的技术或知识 进行改动。而本领域人员所进行的改动和变化不脱离本申请的精神和范围,则都应在本申 请所附权利要求的保护范围内。
Claims (7)
1. 一种反渗透浓缩并且回收利用氯化铵溶液的方法,包括以下步骤: 冷却氯化铵原液; 过滤所述氯化铵原液; 将所述氯化铵原液一次反渗透浓缩得到浓缩氯化铵溶液和渗透液; 冷却所述浓缩氯化铵溶液; 将所述渗透液二次反渗透脱盐得到所述氯化铵原液和第一脱盐水; 其特征在于, 所述第一脱盐水用于冷却氯化铵原液得到第二脱盐水; 所述浓缩氯化铵溶液通过能量回收装置给所述一次反渗透浓缩供给能量; 所述第二脱盐水被所述浓缩氯化铵溶液冷却得到工业用水。
2. 根据权利要求1所述的浓缩并且回收利用氯化铵溶液的方法,其特征在于,冷却后所 述氯化铵原液的温度为15-25°C。
3. 根据权利要求1所述的浓缩并且回收利用氯化铵溶液的方法,其特征在于,所述第一 脱盐水在氯化铵原液中的含量为58%-70%。
4.根据权利要求1所述的浓缩并且回收利用氯化铵溶液的方法,其特征在于,所述第二 脱盐水的温度为60-65°C。
5.根据权利要求1所述的浓缩并且回收利用氯化铵溶液的方法,其特征在于,所述工业 用水的温度为50-55°C。
6.根据权利要求1所述的浓缩并且回收利用氯化铵溶液的方法,其特征在于,所述一次 反渗透浓缩和所述二次反渗透脱盐可采用多段渗透膜。
7.根据权利要求1或6所述的浓缩并且回收利用氯化铵溶液的方法,其特征在于,所述 浓缩氯化铵溶液通过能量回收装置对进入所述渗透膜的溶液进行增压。
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