Journal of Textile Research ›› 2021, Vol. 42 ›› Issue (08): 24-33.doi: 10.13475/j.fzxb.20210301311

• Academic Salon Column for New Insight of Textile Science and Technology: Recycling and Biodegradable Fiber • Previous Articles     Next Articles

Review on treatment technology for typical pollutants in textile industry

ZHANG Yaopeng1,2, SHEN Chensi1,2, XU Chenye1,2, LI Fang1,2()   

  1. 1. College of Environmental Science and Engineering, Donghua University, Shanghai 201620, China
    2. Textile Pollution Controlling Engineering Center of Ministry of Environmental Protection, Donghua University, Shanghai 201620, China
  • Received:2021-03-02 Revised:2021-05-02 Online:2021-08-15 Published:2021-08-24
  • Contact: LI Fang E-mail:lifang@dhu.edu.cn

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Abstract:

With the improvement of the concept of "the construction ecological civilization" and the need for industrial transformation and upgrading, the emission standards and environmental management requirements of textile industry are increasingly more strict. In order to further eliminate the pollution generated by the textile industry, the treatment technologies for the removal of the three typical textile-related pollutants, including heavy metals, sizing regent, dyes and their intermediates, were analyzed and concluded from the aspects of physicochemical, biochemical and advanced oxidation treatments during the textile production and discharge. The efficiency of different treatment technologies to remove pollutants was compared, and the suggestions are given based on the development stage of China. It is pointed out that the development of multi linkage technology of "physicochemical-biochemical-advanced treatment" is the key to the transformation of textile industry to green development, which provide a new ideas for the future green development of textile industry.

Key words: textile industry, heavy metal, sizing regent, dye and intermediate, pollutant, waste water treatment technology

CLC Number: 

  • X1

Tab.1

Summary of reaction conditions and treatment effects for Sb removal"

处理方法 处理条件 废水水质 处理效果 参考文献
混凝沉淀法 PFS 投加量为500 mg/L,pH=9,室温 含锑废水(模拟废水)
ρ(总Sb)=5 mg/L		 总Sb去除率为98.0% [13]
PFS 投加量为30~90 mg/L,pH=6~8,温度为10~25 ℃ 含锑废水(模拟废水)
ρ(Sb(Ⅴ))=20 μg/L		 Sb(V)去除率为98.4% [21]
氯化铁 投加量为4×10-4 mol/L,pH=3~10,室温 含锑废水(模拟废水)
ρ(Sb(III/Ⅴ))=100 μg/L		 Sb(III)去除率为93.0%
Sb(V)去除率为73.0%		 [22]
吸附法 复合藻粉 投加量为0.6 g/L,
pH=7.5,室温		 含锑废水(模拟废水)
ρ(Sb(III/V))=25 mg/L		 qm,Sb(III)=175.8 mg/g
qm,Sb(V)=4.9 mg/g		 [16]
磁性赤铁矿 投加量为100 mg/L,
pH=7,室温		 含锑废水(模拟废水)
ρ(Sb(III))=110 μg/L		 qm,Sb(III)=36.7 mg/g [23]
UiO-66(NH2) 投加量为1 g/L,pH=7,室温 含锑废水(实际废水)
ρ(Sb(III/V))=10 mg/L		 Sb(III)去除率可达99.2%
Sb(V)去除率可达99.1%		 [17]
改性碳纳米管 投加量为2.5 g/L,
pH=5,室温		 含锑废水(模拟废水)
ρ(Sb(III/V))=50 mg/L		 qm,Sb(III/V)=250.0 mg/g [24]
电场辅助吸附 电压为2 V,流速为
1.5 mL/min,pH=7,室温		 含锑废水(模拟废水)
ρ(Sb(III))=100 μg/L		 Sb(III)去除率可达90.0% [18]
电混凝 电压为6 V,电流密度为
10 mA/cm2,pH=2.5,室温		 含锑废水(模拟废水)
ρ(Sb(III/V))=1 mg/L		 Sb(III)去除率可达99.5%
Sb(V)去除率可达97.2%		 [19]
壳聚糖络合超滤 络合反应1 h,pH=6,
装载比为10		 含锑废水(模拟废水)
ρ(Sb(III))=100 μg/L		 Sb(III)截留率可达96.5% [25]

Tab.2

Summary of reaction conditions and treatment effects for Cr removal"

处理方法 处理条件 废水水质 处理效果 参考文献
还原-沉
淀法		 紫外线/过硫
酸盐		 投加量为5 mmol/L,
pH=5~10,室温,无氧		 含铬废水(模拟废水)
ρ(Cr(VI))=5 mg/L		 Cr(VI)去除率可达100.0% [29]
零价铁电化
学法		 投加量为0.08 mg/L,pH=5,室温 含铬废水(模拟废水)
ρ(Cr(VI))=10 mg/L		 Cr(VI)去除率可达95.4% [30]
吸附法 HCM 投加量为0.4 g/L,pH=2,室温 含铬废水(模拟废水)
ρ(Cr(VI))=40~300 mg/L		 qm,Cr(VI)=332.5 mg/g [31]
Fe3O4/Mg(OH)2 投加量为0.4 g/L,pH=10,室温 含铬废水(模拟废水)
ρ(Cr(VI))=10 mg/L		 qm,Cr(VI)=15.5 mg/g [32]
UFB-PPy 投加量为0.5 g/L,pH=2~12,室温 含铬废水(模拟废水)
ρ(Cr(VI))=10~150 mg/L		 qm,Cr(VI)=86.7 mg/g [33]
还原-吸附/
吸附-还原法		 苹果木生物炭 投加量为10 g/L,pH=2,室温 含铬废水(模拟废水)
ρ(Cr(VI))=50 mg/L		 Cr(VI)去除率可达99.9% [35]
PANI/PS 投加量为1 g/L,pH=6,室温 含铬废水(模拟废水)
ρ(Cr(VI))=10~200 mg/L		 qm,Cr(VI)=233.7 mg/g [36]
nZVI/C 投加量为200 mg/L,pH=3,室温 含铬废水(模拟废水)
ρ(Cr(VI))=200~2 000 mg/L		 qm,Cr(VI)=814.9 mg/g [37]
破络-还
原法		 CS-Fe-Cu 投加量为1 g/L,ρ(H2O2)=20 mmol/L,pH=6,室温 含铬废水(模拟废水)
ρ(Cr(III))=5 mg/L
ρ(酸性蓝193)=50 mg/L		 脱色率为100.0%,总铬去除率为90.0%,Cr(VI)最大积累量小于0.1 mg/L [39]

Tab.3

Summary of reaction conditions and treatment effects for textile sizing regents removal"

处理方法 处理条件 废水水质 处理效果 参考文献
聚乙烯醇 Fenton ρ(Fe2+)=30 mmol/L,
ρ(H2O2)=50 mmol/L,
pH=6,室温		 浆料废水(实际废水)
ρ(CODCr)=3 822 mg/L
ρ(PVA)=326 mg/L		 CODcr去除率为50.9%
浊度去除率为99.8%		 [51]
Fenton预处理-钙盐絮凝 ρ(FeSO4·7H2O)=8 g/L,
ρ(H2O2)=0.02 g/L,
ρ(CaCl2)=0.02 g/L,
pH=3.5,室温		 浆料废水(模拟废水)
ρ(PVA)=10 g/L		 PVA去除率为96.0%
CODCr去除率为81.3%		 [48]
自由基交联 ρ(过硫酸钾)=10 g/L,反应温度为70 ℃ 浆料废水(模拟废水)
ρ(PVA)=10 g/L		 PVA去除率大于90.0%
CODCr去除率大于90.0%		 [47]
淀粉 超滤+反渗透 运行压力为0.15 MPa,pH=7~9,室温 染料废水(实际废水)
ρ(CODCr)=7 500~8 000 mg/L
ρ(悬浮物)=800~2 000 mg/L		 CODCr去除率大于98.8%
悬浮物去除率大于99.0%		 [52]
2级上流式厌氧污泥床+厌氧好氧工艺 有机负荷为4 kg/(m3·d),
曝气量为18.53 m3/min,室温		 浆料废水(实际废水)
ρ(CODCr)=1 000~
2 000 mg/L
ρ(氨氮)=10~50 mg/L		 出水CODCr≤93.0 mg/L
出水氨氮≤7.0 mg/L		 [53]
海藻酸钠 Fenton ρ(Fe2+)=8 mg/L,ρ(H2O2)=50 mmol/L,pH=5.3,反应温度为50 ℃ 染料废水(模拟废水)
ρ(海藻酸钠)=15 g/L		 海藻酸钠去除率可达85.2% [54]
上流式厌氧污泥床 有机负荷为6 kg/(m3·d),pH=7~9,自然水温 浆料废水(实际废水)ρ(CODCr)=3 000~7 000 mg/L CODCr去除率平均为80.0% [55]

Tab.4

Summary of reaction conditions and treatment effects for dye removal"

处理方法 处理条件 废水水质 处理效果 参考文献
吸附 改性淀粉 投加量为500 mg/L,pH=3~10,室温 染料废水(模拟废水)
ρ(亚甲基蓝)=200 mg/L		 qm,亚蓝基蓝=157.8 mg/g [56]
金属有机框架 投加量为1 600 mg/L,室温 染料废水(模拟废水)
ρ(罗丹明B)=20~250 mg/L		 qm,罗丹明B =565.0 mg/g [57]
壳聚糖吸附剂 投加量为2 000 mg/L,
中性条件,反应温度为30 ℃		 染料废水(模拟废水)
ρ(活性红紫)=800 mg/L
ρ(活性红)=800 mg/L
ρ(活性黄)=800 mg/L		 qm,活性红紫 =400.0 mg/g
qm,活性红 =398.4 mg/g
qm,活性黄 =404.9 mg/g		 [58]
混凝/絮凝 氢氧化镁混凝 镁离子投加量为150 mg/L,
高岭土投加量为10 mg/L,室温		 染料废水(模拟废水)
ρ(活性橙)=250 mg/L		 染料去除率大于98.0% [59]
氯化铝混凝 投加量为100 mg/L,室温 染料废水(模拟废水)
ρ(分散红)=100 mg/L		 染料去除率可达96.9% [60]
膜分离 纳滤 渗透率为1.26×10-4 L/(h·m2·Pa),运行时间为700 min 染料废水(模拟废水)
ρ(刚果红)=500 mg/L		 截留率可达99.2% [61]
超滤 铸膜液中氧化石墨烯添加量为
0%~0.9%		 染料废水(模拟废水)
ρ(刚果红)=50 mg/L
ρ(NaCl)=1 mol/L		 截留率可达75.2% [62]
化学氧化法 流化床+Fenton
氧化工艺		 ρ(染料)∶ ρ(Fe2+)∶ρ(H2O2)=
1∶0.1∶2.5,pH=3,填料负载量为20 g		 染料废水(模拟废水)
ρ(活性黑5)=500 mg/L		 CODCr去除率为83.0%
色度去除率为99.0%		 [63]
类Fenton 催化剂投加量为1 g/L,
ρ(H2O2)=5 mmol/L,pH=2		 染料废水(模拟废水)
ρ(铬黑T)=50 mg/L		 色度去除率为97.0% [64]
湿式过氧化氢氧化 ρ(H2O2)=0.01 mmol/L,反应温度为150 ℃,反应压力为0.5 MPa 染料废水(模拟废水)
ρ(活性艳蓝)=200 mg/L		 色度去除率为100.0%
总有机碳去除率为68.0%		 [65]
电催化氧化 改性钛电极,电流密度为168.9 A/m2,pH=4.5,室温 染料废水(模拟废水)
ρ(孔雀石绿)=150 mg/L		 色度去除率为99.0%
总有机碳去除率为98.0%		 [66]
电Fenton 改性石墨烯电极,ρ(Fe2+)=0.2 mmol/L,ρ(Na2SO4)=50 mmol/L,pH=3 染料废水(模拟废水)
ρ(酸性橙7)=0.1 mmol/L		 总有机碳去除率为94.0% [67]
臭氧/紫外光 臭氧投加量为8.5 mg/min,pH=11 染料废水(模拟废水)
ρ(直接蓝86)=100 mg/L
ρ(CODCr)=500 mg/L		 CODCr去除率为62.0% [68]
光催化 投加量为1 000 mg/L,300 W氙灯 染料废水(模拟废水)
ρ(亚甲基蓝)=30 mg/L		 亚甲基蓝降解率为98.6% [69]
紫外光/过硫酸盐 ρ(过硫酸钾)=50 μmol/L,pH=2 染料废水(模拟废水)
ρ(罗丹明B)=10 μmol/L		 色度去除率为100.0%
总有机碳去除率为60.0%		 [70]
生物法 固定床生物
反应器		 水力停留时间为3 h,容积负荷为
1.7 kg COD/(m3·d),气水比为1.5∶1,温度为30℃		 染料废水(模拟废水)
ρ(活性艳红)=50 mg/L		 CODcr去除率为88.2%
色度去除率为87.4%
UV254去除率为76.6%		 [71]
厌氧析流板反应器(ABR) ρ(混合液挥发性悬浮固体)=15.6 g/L,ρ(混合液悬浮固体)=32.5 g/L,水力停留时间分别为32、24、18、14和10 h 印染废水(实际废水)
ρ(CODCr)=517 mg/L
ρ(BOD5)=95 mg/L
色度为380倍
pH=8.37		 CODCr最大去除率为46.1%
色度最大去除率为63.5%		 [72]
偶氮染料脱色菌 ρ(氯化铵)=1 g/L,ρ(葡萄糖)=2 g/L,厌氧条件,温度为30~40 ℃, pH=7~9 染料废水(模拟废水)
ρ(酸性红B)=80 mg/L		 色度去除率可达98.73% [73]
小球藻 昼夜比为1∶1,pH=7.2,室温 印染废水(实际废水)
ρ(BOD5)=630 mg/L
ρ(氨氮)为347 mg/L
ρ(Cl-)=847 mg/L		 色度去除率可达85.0% [74]

Tab.5

Summary of reaction conditions and treatment effects for aniline removal"

处理方法 处理条件 废水水质 处理效果 参考文献
磁性树脂吸附 投加量为800 mg/L,pH=5,
温度为30 ℃,吸附时间为3 h		 苯胺废水(模拟废水)
ρ(苯胺)=100 mg/L		 苯胺去除率大于80.0% [86]
混凝/絮凝+气浮 药剂投加量为20 mg/L,絮凝时间为10 min,
气浮时间为20 s,压力为0.4 MPa,pH=6		 苯胺废水(模拟废水)
ρ(苯胺)=200 mg/L		 苯胺去除率为95.0%
CODCr去除率为89.6%		 [87]
TiO2/紫外-H2O2 催化剂投加量为320 mg/L,H2O2投加量为1%,紫外光灯功率为150 W,回流比为50% 苯胺废水(实际废水)ρ(CODCr)=700~1 100 mg/L
色度为1 000~1 500倍		 出水CODCr≤60.0 mg/L
色度≤20.0倍		 [88]
微生物电
池-Fenton		 Ag/AgCl电极,pH=7.2,室温,
曝气量为16 mL/min,电压为0.5 V		 苯胺废水(实际废水)
ρ(苯胺)=4 460 mg/L
ρ(总有机碳)=3 360 mg/L		 苯胺去除效率为30.0 g/(L·h)
总有机碳去除率为93.1%		 [89]
A2/O 好氧型8%+厌氧型4%包埋菌,污泥回流比为70%~80%,硝化液回流比为200%,
水力停留时间为24 h		 苯胺废水(模拟废水)
ρ(苯胺)=60 mg/L		 CODCr去除率大于90.0%
总氮去除率为76.2%
氨氮去除率为91.0%		 [85]
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