反渗透系统运行指标的标准化方法

介绍了反渗透系统运行指标标准化的意义,分析了修正系数法标准化的数学模型及其存在的问题,提出了膜元件与污染层双重动态特性的概念,明确了动态特性方法的计算过程及应用优势。     

反渗透系统中膜元件安装位置的优化排列

提出了反渗透系统中膜元件位置优化排列的概念;分析了膜元件的产水量、透盐率及膜压降三项指标的离散特性;明确了膜元件位置优化排列的数学方法;实例计算了离散特性膜元件优化排列的系统运行效果。     

恒应变率下的岩石三轴动态变形过程模拟方法

针对岩石动态变形特点,首先引进Kelvin模型研究思路与方法,将岩石变形过程中的动态应力视为静态应力分量与动态应力分量的叠加,分别以黏性元件和非线性元件模拟岩石单元的动态应力分量与静态应力分量,并建立出岩石动态应力的力学分析模型;然后在此研究基础上,利用黏性元件的力学特性和统计损伤理论分别建立出黏性元件和非线性元件变形过程模拟方法,进而得到岩石三轴动态变形过程模拟方法,并提出其模型的参数确定方法;最后通过实例分析与讨论,表明该模型不仅能反映岩石动态变形过程的应变软化特性,而且能较好地反映加载速度或应变率对岩石三轴动态变形过程的影响,具有较强的合理性和可行性。     

纳滤膜元件的运行特性分析

通过对影响纳滤膜元件性能的给水温度、膜通量及含盐量3项重要因素进行的正交设计试验,分析了不同脱盐率纳滤膜元件的工作压力和透盐率的给水温度、给水含盐量及膜元件通量的特性,并明确了不同脱盐率纳滤膜元件工作压力及透盐率的回收率特性,从而为建立特定系列纳滤膜元件的连续运行特性图谱提供了一个典型模式。     

基于组合模型法的贯通节理岩体动态损伤本构模型

针对贯通节理岩体动态变形特点并结合已有岩石动态本构模型的相关研究成果,将贯通节理岩体变形过程中的动态应力视为贯通节理岩体静态应力分量与相应动态应力分量的叠加。其中贯通节理岩体静态应力分量采用考虑岩石细观损伤的非线性元件、节理面闭合及剪切变形元件等3个基本元件的串联来模拟,动态应力分量采用黏性元件来模拟,从而建立了贯通节理岩体动态单轴压缩损伤本构模型。其次,根据贯通节理岩体在单轴压缩荷载下往往会沿节理面发生剪切破坏的特点,在前述已建立的损伤本构模型中引人节理剪切破坏准则对该模型进行修正,从而更好地考虑了节理剪切强度对该模型的影响,最终建立了考虑节理剪切强度的贯通节理岩体单轴压缩损伤本构模型。最后利用该模型对贯通节理岩体在压缩荷载作用下的力学特性进行了分析计算,重点讨论了节理倾角对岩体单轴动态压缩峰值强度的影响规律。研究结果表明随着节理倾角的变化,节理岩体将发生岩块张拉或剪切破坏、沿节理面的剪切破坏及上述两种破坏模式的复合破坏,相应地节理岩体的单轴压缩动态峰值强度也随之有较大变化。     

污水深度回用反渗透膜面微生物污染机理试验研究

微生物污染是最复杂的膜污染形式,是污水深度回用反渗透设备运行过程关注的焦点.通过实验室静态试验和错流过滤动态试验研究了污水回用反渗透膜的微生物污染的机理和特性,结果表明:造成污染的微生物主要为杆菌和丝状菌;在没有微生物源及没有微生物生长和繁殖的必需营养物质的情况下,膜面基本不发生微生物污染;杀菌处理对于防止微生物污染很重要,已经污染的膜面更易于发生微生物污染,做好反渗透设备的停备用保护工作是防止微生物污染的必要手段.     

平衡阀的研究和试验

平衡阀在液压执行元件(马达或缸)的下降管路中起着建立背压、平衡外载荷的重力作用,从而保持载荷的位置或者控制载荷的下降速度,是工程起重机液压系统的重要元件,它关系到整个起重机工作的平稳性、可靠性和系统效率。为了满足起重机的性能要求,平衡阀本身必须具有工作稳定、不发生振动和冲击、动作灵敏、随动性好、有较宽的流量控制范围、控制压力不能过高、闭锁可靠等优点。总之,要求它具有良好的静态特性和动态特性。平衡阀的静态特性一般指研究阀内各工作零件在静态力作用下的平衡关系,相当于起重     

工程液压阀通用试验台

本文以阀类元件通用试验台为例，着重介绍了液压阀通用试验台的设计原理和构思，以及阀类元件静态试验所需的基本功能回路。     

减轻液压油污染的有效措施

液压系统是否正常,直接关系到工程机械能否正常工作,而液压油的污染程度与液压系统的故障有直接的关系。 固体颗粒污染物会加剧液压元件的表面腐蚀和磨损,增大泄漏量,使油温升高、压力下降、效率     

反渗透膜元件的动态性能参数检测方法

分析了反渗透膜元件性能的影响因素及动态特点,给出了反渗透膜元件透水因子与透盐因子的数学模型,明确了两个透过因子多项式模型的参数求解过程与简化计算过程,并提出了反渗透膜元件动态性能参数试验检测的理论与方法.     

反渗透膜元件透过系数的试验与数学求解

明确了反渗透膜元件两透过系数求解所需的函数形式、幂项数、试验组数、试验点位、变量归一、回归分析及回归效果检验等一系列试验与数学过程,并给出了某支膜元件两透过系数求解的试验数据及其计算实例。     

脊谷式张拉膜结构风振特性分析

张拉式膜结构属风敏感体系,对其在脉动风荷载作用下的动力性能进行准确评估一直是该类结构设计中的重要内容．但国内以往在这方面的研究较少,该问题一直没有很好地解决．本采用非线性随机模拟时程分析方法对张拉式膜结构的典型形式之一——脊谷式膜结构的风振响应特性进行系统的参数分析,探讨了来流特性、跨度、高跨比、膜预张力等参数对结构动力性能的影响．在此基础上,本提出了一种针对于张拉膜结构特点的抗风设计方法．     

索膜结构中考虑摩擦的索滑移分析

以第一摩擦定律为理论基础,首先利用空间三角形膜单元并根据材料力学点的应力应变关系推导出在局部坐标系下索元对膜元的拉力公式;其次根据索与膜的位置关系推导出索膜间摩擦力的公式;然后提出了考虑摩擦时索滑移的判断方法;最后利用荷载增量法与Newton-Raphson法相结合的迭代求解方法,并结合索滑移的算法求解了一道算例,得到在索与膜之间的摩擦力虽对结构的静力影响不大,但摩擦力的存在却影响着膜褶皱出现的数量和索的下料长度,所以设计时应考虑摩擦力的影响等结论。     

Full-scale simulation of seawater reverse osmosis desalination processes for boron removal: Effect of membrane fouling

The objective of this study is to further develop previously reported mechanistic predictive model that simulates boron removal in full-scale seawater reverse osmosis (RO) desalination processes to take into account the effect of membrane fouling. Decrease of boron removal and reduction in water production rate by membrane fouling due to enhanced concentration polarization were simulated as a decrease in solute mass transfer coefficient in boundary layer on membrane surface. Various design and operating options under fouling condition were examined including single- versus double-pass configurations, different number of RO elements per vessel, use of RO membranes with enhanced boron rejection, and pH adjustment. These options were quantitatively compared by normalizing the performance of the system in terms of E_min, the minimum energy costs per product water. Simulation results suggested that most viable options to enhance boron rejection among those tested in this study include: i) minimizing fouling, ii) exchanging the existing SWRO elements to boron-specific ones, and iii) increasing pH in the second pass. The model developed in this study is expected to help design and optimization of the RO processes to achieve the target boron removal at target water recovery under realistic conditions where membrane fouling occurs during operation.     

Combined coagulation-disk filtration process as a pretreatment of ultrafiltration and reverse osmosis membrane for wastewater reclamation: an autopsy study of a pilot plant

The effects of the combined coagulation-disk filtration (CC-DF) process on the fouling characteristics and behavior caused by interactions between effluent organic matter (EfOM) and the membrane surfaces of the ultrafiltration (UF) and reverse osmosis (RO) membranes in a pilot plant for municipal wastewater reclamation (MWR) were investigated. The feed water from secondary effluents was treated by the CC-DF process used as a pretreatment for the UF membrane to mitigate fouling formation and the permeate from the CC-DF process was further filtered by two UF membrane units in parallel arrangement and fed into four RO modules in a series connection. The CC-DF process was not sufficient to mitigate biofouling but the UF membrane was effective in mitigating biofouling on the RO membrane surfaces. Fouling of the UF and RO membranes was dominated by hydrophilic fractions of EfOM (e.g., polysaccharide-like and protein-like substances) and inorganic scaling (e.g., aluminum, calcium and silica). The desorbed UF membrane foulants included more aluminum species and hydrophobic fractions than the desorbed RO membrane foulants, which was presumably due to the residual coagulants and aluminum-humic substance complexes. The significant change in the surface chemistry of the RO membrane (a decrease in surface charge and an increase in contact angle of the fouled RO membranes) induced by the accumulation of hydrophilic EfOM onto the negatively charged RO membrane surface intensified the fouling formation of the fouled RO membrane by hydrophobic interaction between the humic substances of EfOM with relatively high hydrophobicity and the fouled RO membranes with decreased surface charge and increased contract angle.     

Combined influence of membrane surface properties and feed water qualities on RO/NF mass transfer, a pilot study

The impact of membrane surface characteristics and NOM on membrane performance has been investigated for varying pretreatment and membranes in a field study. Surface charge, hydrophobicity and roughness varied significantly among the four membranes used in the study. The membranes were tested in parallel following two different pretreatment processes, an enhanced Zenon ultrafiltration process (ZN) and a compact CSF process (Superpulsator (SP)) prior to RO membrane treatment for a total of eight integrated membrane systems. All membrane systems were exposed to the similar temperature, recovery and flux as well as chemical dosage. The membrane feed water qualities were statistically equivalent following ZN pretreatment and SP pretreatment except for NOM and SUVA. Membrane surface characteristics, NOM and SUVA measurements were used to describe mass transfer in a low-pressure RO integrated membrane system. Solute and water mass transfer coefficients (MTCs) were investigated for dependence on membrane surface properties and NOM mass loading. Inorganic MTCs were accurately described by a Gaussian distribution curve. Water productivity decreased with NOM loading and increased with contact angle and roughness. The negative effects of NOM loading on productivity were reduced as the negative charge on the membrane surface increased. Inorganic MTCs were also correlated to surface hydrophobicity and surface roughness. The permeability change of identical membranes was related to NOM loading, hydrophobicity and roughness. Organic fouling as measured by water, organic and inorganic mass transfer was less for membranes with higher hydrophilicity and roughness.     

膜法水处理技术的最新进展

详细介绍了2007年5月在英国Harrogate召开的“第4届IWA国际膜会议：膜法水与废水处理”的情况。对会议发表的宣读论文。从膜生物反应器、微污染水的低压膜过滤和NF／RO等方面进行了讨论，介绍了最近两年来国际上相关领域的最新研究进展。从此次膜会议来看，膜生物反应器尤其是好氧膜生物反应器仍是目前研究的热点，其中针对膜污染的机理、应对措施以及MBR节能降耗的研究最多，并取得了很多新的认识和切实有效的措施。     

双膜法在市政污水处理厂的应用

天津市某污水处理厂再生水回用工程采用双膜法工艺,近期设计规模为2.0×10^4m^3/d,本文介绍了其工艺流程、设备配置情况、工程设计参数等.运行结果表明,采用双膜法对废水进行处理后出水水质良好,可以达到回用标准,其中超滤出水浊度为0.01～0.04 NTU,反渗透产水电导率＜ 15 μs/cm,脱盐率大于99％.经济性分析结果显示,该双膜法再生水回用工程的吨水运行成本为1.584元,具有良好的经济及环境效益.