商业正渗透膜的改性及其用于处理焦化废水的研究

doi:10.11949/0438-1157.20190670

摘要/Abstract

摘要：

正渗透技术是一种新兴的膜分离技术，在处理有机废水方面具有广阔的应用前景。分别对Poten以及HTI商业正渗透膜进行改性，并用于对焦化废水中难降解毒性小分子(吲哚和吡啶)的截留测试。探究了水相单体PIP浓度、膜朝向、汲取液浓度对改性前后两种膜水通量、J_s/J_w比值、有机物截留率的影响，以及改性前后两膜特征参数的变化。结果表明：对Poten膜和HTI膜进行界面聚合改性后，膜水通量以及J_s/J_w比值都不同程度地降低；改性后的两正渗透膜水渗透系数A、盐渗透系数B均降低，而膜结构参数S以及对NaCl和有机物的截留率均提高；其中HTI-IP复合膜对有机物的截留率(81%)明显高于IP-2(改性Poten膜)复合膜；与FO模式相比，IP-2复合膜在PRO模式下(汲取液面向活性层)具有更高的水通量及反向盐通量。此外，在两种膜朝向下，水通量及反向盐通量都随汲取液浓度的增大而增大，但是在FO模式下(料液面向活性层)，通量呈现非线性增长。

关键词: 正渗透膜, 焦化废水, 改性, 界面聚合

Abstract:

Forward osmosis technology is an emerging membrane separation technology and has broad application prospects in the treatment of organic wastewater. In this paper, the Poten and HTI commercial forward osmosis membranes were modified and used for the rejection of refractory toxic small molecules (indole and pyridine) in coking wastewater. The effects of PIP concentration, membrane orientation and draw solution concentration on the membrane water flux, J_s/J_wratio and organic matter rejection before and after modification, and the changes of the membrane characteristic parameters before and after modification were investigated. The results show that the membrane water flux and the J_s/J_w ratio are reduced to different degrees after the interfacial polymerization modification of the Poten membrane and the HTI membrane. The water permeability coefficient A and the salt permeability coefficient B of the modified two forward osmosis membranes were both reduced. The membrane structure parameter S and the rejection of NaCl and organic matters were improved; the rejection of organic matter by HTI-IP composite membrane (81%) was significantly higher than that of IP-2 composite membrane; compared with FO mode, IP-2 composite membrane had higher water flux and reverse salt flux in PRO mode. In addition, both water flux and reverse salt flux increase with increasing draw solution concentration in different membrane orientations, but in FO mode, membrane flux exhibits a non-linear increase.

Key words: forward osmosis membrane, coking wastewater, modification, interfacial polymerization

中图分类号:

TQ 028

李志强, 吕娜, 蒋兰英. 商业正渗透膜的改性及其用于处理焦化废水的研究[J]. 化工学报, 2020, 71(S1): 461-470.

Zhiqiang LI, Na LYU, Lanying JIANG. Modification of commercial forward osmosis membranes and investigation on treatment of coking wastewater[J]. CIESC Journal, 2020, 71(S1): 461-470.

图/表 17

表1 模拟焦化废水的组成（pH=7.5）

Table 1 Composition of simulated coking wastewater(pH=7.5)

成分	浓度/(mg/L)
吲哚	50
吡啶	50
NH₃-N	80
COD	146

图1 自制框式界面聚合装置

Fig.1 Self-made frame interface polymerization device

图2 Poten膜界面聚合反应

Fig.2 Schematic of interfacial polymerization reaction of Poten membrane

图3 HTI膜界面聚合反应原理

Fig.3 Principle of HTI membrane interfacial polymerization reaction

图4 正渗透过程原理图1—料液罐；2—电导率仪；3—磁力泵；4—流量计；5—膜组件；6—压力表；7—汲取液灌

Fig.4 Schematic of forward osmosis process

图5 实验室自制RO设备1—料液罐；2—磁力泵；3—压力表；4—膜组件；5—阀门；6—渗透液罐；7—流量计；8—电子秤

Fig.5 Lab-made reverse osmosis equipment

图6 PIP单体浓度对Poten膜正渗透性能的影响

Fig.6 Effect of PIP monomer concentration on FO performance of Poten membrane

图7 不同PIP浓度改性后Poten膜的SEM图

Fig.7 SEM images of Poten membrane after modification of different PIP concentrations

图8 不同PIP浓度改性后Poten膜的AFM结果

Fig.8 AFM results of Poten membrane after modification of different PIP concentrations

图9 不同PIP浓度改性后的Poten膜接触角变化

Fig.9 Contact angle change of Poten membrane after modification of different PIP concentrations

图10 改性前后HTI膜正渗透性能（a）以及接触角（b）变化

Fig.10 FO performance(a) and contact angle (b) change of HTI membrane before and after modification

图11 改性前后HTI膜SEM图

Fig.11 SEM images of HTI membrane before and after modification

图12 改性前后HTI膜AFM结果

Fig.12 AFM results of HTI membrane before and after modification

表2 改性前后正渗透膜的特征参数测试结果

Table 2 Test results of characteristic parameters of FO membrane before and after modification

样品	A/(kg/(m²·h·bar))	B/(kg/(m²·h))	S/μm	R/%
PIP-0	7.64	0.264	882	87.2
PIP-2	5.43	0.071	1543	94.7
HTI	0.36	0.0035	278	93.0
HTI-IP	0.33	0.0011	581	98.0

图13 改性前后两FO膜对有机物截留率的变化

Fig.13 Changes in organic matter rejection of two FO membranes before and after modification

图14 PIP-2膜通量随汲取液浓度的变化(FO模式)

Fig.14 PIP-2 membrane flux change with draw solution concentration (FO mode)

图15 PIP-2膜通量随汲取液浓度的变化(PRO模式)

Fig.15 PIP-2 membrane flux change with draw solution concentration (PRO mode)

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