环境工程专业毕业设计外文翻译

介绍： (1)

1实验性 (2)

1.1污水和活性污泥 (2)

1.2实验性设定和过程 (3)

1.3测试和监视抽样采取从混杂的醇中过滤 (4)

2.结果 (5)

2.1泥浆化颗粒化 (5)

2.2 EGSB操作流出物的稳定酸碱度 (6)

3 .TPD污水的理论演算和讨论 (7)

3.1酸平衡和中间转换能力酸碱度 (7)

3..2VFA在厌氧过程用二种主要方式的二个主要小组细菌介入降低有机基体 (8)

3..3VFA和强碱性平衡强碱性的典型的变异 (8)

4.结论 (9)

命名原则 (10)

参考文献 (10)

Introduction (12)

1Experimental (14)

2 Results (16)

3 Theoretical calculation and discussions (19)

4 Conclusions (22)

recomference: (23)

稳定性的膨胀的颗粒状污泥床

对涤纶人造丝印染废水的处理

摘要

涤纶人造丝印染污水(TPD污水)，包含平均7.0mg/L对苯二甲酸（技术援助）作为主要碳来源和特性污染物，从属于膨胀的颗粒状污泥床(EGSB)过程。EGSB过程的稳定由实验室实验首先研究了。TA电离是影响系统的酸基度平衡的优势的因素。废水的 TA 的高集中造成充份的缓冲能力使中立脂肪酸 (VFA) 从培养基降格产生而且提供了没有空气而能生活强的系统挥发性基础抵抗 pH 减少到低于6.5 。挥发性脂肪和不饱和脂肪酸除每小时次于6.35和挥发性脂肪积极从事它的极大值以外几乎没有抑制上去沼气生产。与颗粒化被激活的污泥一起,有机撤除效率和沼气的生产率逐渐增加了和变得更加稳定。在启动后,COD撤除效率增加到57%-64%,酸碱度被稳定在范围的7.99～6.04,和沼气的生产率是相对高。酸碱度污泥颗粒化的,适当的流入物和装载使EGSB过程稳定。EGSB反应器是稳定的为TPD废水处理。

关键词:膨胀的颗粒状泥床;稳定;绝氧处理;印染污水

介绍：

为了获得柔韧的和优雅的如丝一样涤纶结构、涤纶本色布总是同碱分解过程被预先处理, NaOH以某一温度和压力涤纶纤维被水解在某种程度上。在这个过程期间,表面涤纶纤维从本色布料上被溶化,涤纶酸(TA)和1,2-亚乙基二醇被释放作为污水中主要污染物。获得的充满丝质皱痕和软质感涤纶织品叫做人造丝织品。涤纶的碱分解可能由化工等式描述如下。

污水碱分解过程与污水混合了从打印，洗染，漂洗和其他过程被命名为涤纶人造丝印染的污水(T/D污水)。只在中国东部绍兴县, ,那里每天释放超过300数以万计吨TPD污水。虽然缺氧的或好氧的生化处理已经作为通常的预先为处理的这种废水的方法。多样的曝气过程结构也是它们的一种用法。然而广泛应用的曝气过程已经妨害由缺乏了解到相关因素稳定性的生物进程包括去除系数的有机底质、沼气生产比率和另一些指标。那个包含于稳定性加工的、依靠酸碱平衡特征污染物在吨/日废水的TA是一种二重的有机酸、存在于进水形成分子或离子状态。酸碱平衡在厌氧的体系是静止的大约是由于TA的效果。那展开粒状污泥床（egsb）处理发展从上流式厌氧污泥层处理、是一个有较高的比率和有害的阻力的厌氧控制处理方法。未来的egsb技术发展的由于吨/日废水处理依赖透处理的稳定性。处理的稳定性是论述、酸碱平衡是强调和实验室实验是传导。

1实验性

1.1污水和活性污泥

因为3650吨/日TPD废水在绍兴县、浙江省、瓷器在最上级全年的调查以后废水在实验中是降低那中央的泵站处理率、主要的指标是废水中的污染物是TPD废水以每小时化学需氧量高、化学需氧量和色度为特征，与传统的印染废水COD从780mg／L的到3116mg／L的量不同；和生物需氧量因为（五日生化需氧量）从325mg／L的到1436mg ／L不同，TA从286mg／L的到1279mg／L不同。特征污染物控制在4068COD的3650吨

/日废水活性污泥实验是从杀虫剂废水、印染废水和石炭酸废水污泥处获得。处理设备在实验室厌氧的反应器和egsb反应器到保持高浓度的生物资源的情况一样。

1.2实验性设定和过程

圆柱状的EGSB反应器被划分了成四隔间(图2):

(1)粒状污泥积聚区；（２）液化区；（３）三相分离器（４）粒状污泥床。在那粒状污泥床上、由于废水在粒状污泥的再循环床和液化区，所以液化区发展主要是生物降解发生和沼气生产的地方。当做混合溶液穿过气体液体固体分离器、那污泥穿过分离器的孔到那液化区和污泥场、在一些絮凝和分散污泥泥沉淀反应器同流出的的时候、那表面水流变成存储器从堰流出，并且沼气流入一湿式气体流量计反应器。反应器(图2)是1.5米高的与流化的区域和污泥床f7.0升有效的容积和2.0升的设置隔间。

实验性设定的一张概要图被显示在图31为了从消除高酸碱度和短缺N和P,培养的污水中第一次集中调整了COD:N:P=200:5:1。在污水水库被增加氢磷酸盐和氨硫酸盐和增加稀释盐酸在中立化反应器由滴定器控酸碱度=10.0。泵被连续使用提供污水给

EGSB反应器中混杂的积累污泥有能力在碳上退化。反应温度被加热器和温度调解器控制了。酸碱度被定器(DL55,Mettler?Toledo,德国)监测了和调整了。而滴温度一根热探针连接到一台红外光芒加热器所确定。其它项目的根据标准方法(中国1997环境保护局编辑委员会) 进行了测试。在EGSB反应器的起动期间,磷酸盐和碳酸盐包含Fe、Al,Ni 等增加入混杂的矾花提高被激活的污泥颗粒化。TPD流入物使污水比率逐渐增加到100%。过程稳定被重视当起动由逐步增加举办了污泥负荷和水力负荷。在EGSB反应器起动期间,它被管理在流入物酸碱度6.3～6.8和水力装载0.002～64m3/(m3d)和往上流动线性速度0-2.0m/h,与温度被控制在33～6(Table2)。通常,开始阶段为厌氧过程能被定义作为过渡阶段在反应器之前平稳地运转。参量表明反应器表现在起动期间包括污染物撤除效率,沼气生产率,酸碱度,集中的变异VFA等等。在EGSB反应器起动以后,它被管理在流速大约7.5LPd和HRT32h在EGSB,1h在中立化反应器里,当水力负荷22～609m3/(m3d)和往上流动线性速度1.0～6.0m/h和温度受控在33～6(表2)。厌氧反应器的稳定是以COD撤除效率、沼气生产率和PH值来评价的。所有这些参量取决于酸基地平衡在反应器稳定性。如此总强碱性,VFA和TA集中并且被测试了。

1.3测试和监视抽样采取从混杂的酒立刻被过滤了

对TA的分析是用一台高性能液体色谱分析仪(HPLC,Gilson,法国)测定的。运行以流动相(v/v)在58/42,和加法2～6被集中的H3PO4每公升。分离进行在1.5ml/min流速和专栏温度25～6使用ODS218反回阶段column(Alltech,美国)。一台紫外探测器以波长在254毫微米被使用了。测量出来,TA保留时间是在4.57～6.63分钟。

2.结果

2.1泥浆化颗粒化

泥浆化颗粒化并且EGSB反应器起动起动是EGSB反应器烂泥的过程颗粒化(Hulshoff1986) 的根本。起动经常采取2～6几个月,长期的有一年(Juragen1990)。流入物COD和TA是各自地受控在1250～61943mg/L和563～6.41mg/L,。水力负荷对对污泥稳定进行了调整。图4显示污泥在反应器起动期间在30天和60天特征。被激活的污泥看来分明是异种的反应器,能被划分成污泥床,污泥暂停的区域并且设置区域在天60.Granular烂泥直径是1.0毫米占领超过在EGSB反应器里60天的总烂泥的10%。

反应器中基体含量被显示在图5。在0.4m高度之上,COD集中在设置区域。从底部对0.4反应器的m轴向高度,COD集中退出了。COL出现同COD一样。COD撤除效率增加了从23.6%在30天到49.1%在60,天和COL撤除效率被增加从60%在30天到75.0%在60天。反应器表现改变了污泥颗粒化。EGSB反应器为TPD废水处理通常起动器。生物降解首要发生了在污泥床,并且外部圈导致密集混合污水在EGSB反应器里。

2.2 EGSB操作流出物的稳定酸碱度

使用表明EGSB反应器COD去除效率(～6COD)并且沼气生产率(Vg,相当数量沼气从1公斤COD去除在标准状态之下)。图6显示EGSB的表现变异在起始的期间。从10天到28天,TPD污水在流入物成比例地增加。～6COD的第一高峰价值被提出了在15天和20天之间,与Vg0.11～6.18m3/(kgCOD)。COD去除效率和沼气生产率是不稳定的,和TPD污水流入物在过量地增加了。从28天,流入物是所有TPD污水。在30天和45天之间,流出物酸碱度是7.45～6.05～6COD是36%～69%并且Vg是0.015～

6.20m3/(kgCOD)。流出物酸碱度、～6COD和Vg的变异是在45天之前卓越的。这是一个分化期间为被激活的污泥。在45天以后,流出物酸碱度被稳定在

7.99～6.04～6。COD的范围增加到57%～64%,Vg并且保留了0.12～6.17m3(的稳定的价值kgCOD)。实际上,从45天,粒子污泥从污泥中被区分,EGSB反应器提出了它的更好的稳定。颗粒状污泥被测量,弥补了总污泥的在60天10%。当只采取了反应器cubage的25%污泥床被填满以总污泥的65%。EGSB反应器～6表现改善了和变得稳定与污泥一起颗粒化。它是显著的,COD去除效率总是在75%以下。因为TA依然是作为在厌氧条件下以转交在31.4%和56.0%(Guan之间,2003)慢慢地生物可分解的基体。EGSB反应器在温度20～65三个月，操作保留在停滞的状态为45d。图7说明反应器再开始，沼气生产率逐步被增加。COD去除以40%～60%的效率是相对地稳定。反应器再开始只采取12d。在COD的最大转交率平均为60%之后,系统被交换了对负荷冲击以更高的水力负荷。尽管在16天内200%是正常负荷。沼气生产消沉是由于可怕的负荷。COD去除效率在厌氧系统接受了过量的负荷之后减少了几天滞后。结果说明,EGSB反应器表现能当操作参量很大地改变了不稳定的。在一个星期恢复了对55%～62%的一个正常水平,沼气生产在10d恢复了对0.11～60.15m3/(kgCOD)的正常水平。

3 .TPD污水的理论演算和讨论

3.1酸平衡和中间转换能力酸碱度

酸平衡和中间转换能力酸碱度是最重要的参量。当中一个表明厌氧系统的稳定。细菌的最佳的酸碱度为从6.5到7.5(Souza1986)。当VFA积累导致酸碱度减退,厌氧处理的效率明显已经下降(顾1993)。所以,它在厌氧系统对控制VFA是比对控制酸碱度重要。强碱性被看成如同抵抗VFA储积一个重要角色以便增加一个厌氧系统酸碱度(Kroeker1979年;顾,1993)。污水的强碱性被定义作为可能适合与强的酸的起反应总物质。强碱性包括许多碱组分譬如碳酸盐、重碳酸盐、含水物和有机基物。它们在污水中(叫作为总强碱性中国1997环境保护局编辑委员会)。TPD污水有复杂组分并且碳酸盐、重碳酸盐和含水物的集中无法适当被获得。如此总强碱性在污水被使用来作为重大显示为基本的组分。共同地,混杂的酸2基点平衡在厌氧反应器里由电离平衡氨、VFA和碳酸盐控制(KroekerEJ1979年;张,1997)。氨电离平衡作为等式(2):NH3H2.O=NH++OH-。

(2)当[H+]增加,酸碱度减少并且平衡转移在右边。在35～6,电离常数是1.85～60-5VFA 通常由乙酸和酸组成。因为二VFA有接近的电离常数,电离平衡可能被简化作为乙酸电离被说明在等式(3):CH3COOH=CH3COO-+H+。(3)当[H+]增量,平衡转移到左边并且使成为挥发性酸(UVA)集中增加。在35～6,电离常数是1.73～60-5。当UVA集中增加在

10mg/L之上,作试验者趋向失败(Kroeker1979)。碳酸盐电离平衡被阐明作为等式

(4)H2CO3=HCO-+H+=CO-+2H+。(4) 在一个厌氧系统酸基点平衡并且包括在液体气体阶段之间二氧化碳溶化平衡, 在液体坚实阶段之间碳酸盐平衡和磷酸盐,其它盐电离平衡。它被解释为由于低集中硫氢化物和正磷酸的酸共同地只提供有限的缓冲能力

(Capri1975)。氨和VFA缓冲能力当酸碱度从6.0到7.7变化了可能被忽略,并且厌氧系统的缓冲能力起因于碳酸的电离。如此酸碱度和酸基本的平衡由碳酸和碱电离控制。后者由VFA、氨和另一强的酸和碱合成。NH3-N被测试。PO3-4的集中的范围-P和硫化物是1.81～64.45mg/L,1.78～60.20Mg/L并且0.76～6.21mg/L相应地, 各自的平均值是10.23,4.26和2.12mg/L,。根据以前的工作以上提到,氨缓冲能力,磷酸盐和氢硫酸在TPD

污水可能被忽略。然后,哪个负责对酸2base平衡的中间转换？当EGSB过程向被应用的TPD污水～6在这样一个碳酸系统怎么获得稳定的酸碱度。以6.5～6.5的范围～6TA 是双重有机酸,存在在水中以分子或离子状态二个状态。进一步来说,它的可溶性与酸碱度密切相关。电离平衡被显示得如下(百科全书编辑委员会化工业1990):

3.2VFA在厌氧过程用二种主要方式的二个主要小组细菌介入降低有机基体

在第一阶段对挥发性脂肪酸(VFA)水解和降低复杂有机基体。在第二阶段,VFAs 由细菌运用并且导致甲烷气产生。二个过程同时发生并且过程稳定取决于在二个主要阶段之间有机基体细微生物化学的平衡。厌氧处理不稳定通常以由VFAs的集中的迅速增量而甲烷气生产的随后减退表明。有许多因素与相关不稳定或过程破坏。例如,甲烷的不足的生理适应对新基体、迅速温度或酸碱度波动。从结果由Kroeker等。(Andrews1969年;Kroeker,1979),厌氧消化毒力与挥发性酸的过份集中关系了(UFAs)更加直接,虽然它们与过份游离氨含量大概间接地关系了。而且,以由于膜法酸碱度比其它化合物容易击穿通过细胞膜毒力有一种接近的交互作用。当微生物同化污泥，酸碱度使细胞迅速地下降并且微生物的新陈代谢率减少。它是可接受的,作试验者毒力由膜法造成在集中在30到60mg/L之上作为乙酸。

3.3 VFA和强碱性平衡强碱性的典型的变异

VFA和强碱性平衡强碱性的典型的变异和VFA在EGSB反应器里被显示在图11。缺氧流出物的强碱性集中与TPD污水在900～6000mg/L的范围近似地相等的。反弹范围是大约100mg/L。在EGSB的处理以后总强碱性集中增加了大约250mg/L到1150～6250mg/L。流入物(TPD污水)VFA90～633mg/L增加到197～636mg/L在缺氧处理以后,当流出物VFA以去除效率79.1%～62.1%从EGSB反应器是19.8～63.2mg/L。总强碱性增量在EGSB反应器里能被假定与VFA的消耗量相关。

强碱性是在厌氧系统缓冲抵抗VFA能力。污水的VFA几乎抑制不了厌氧过程。强碱性的集中是缓冲VFA足够高的混杂的醇。Lesilie(Lesilie1989)采取为VFA比与总强碱性评估缓冲厌氧能力system(Leslie,1989)。总强碱性轻微只下降了在缺氧治处理期间和在EGSB反应器里轻微登升高。VFA的定量对total2.alkalinity比0141VFA比和总强碱性与相关厌氧系统的稳定被显示在表3 (Leslie1989)。明显地, 当TPD污水在EGSB 反应器里处理时VFA集中的变异只导致了酸碱度的少量变化。混杂的醇的缓冲能力在EGSB过程是充足的。

4.结论

TA,二重的有机酸因为酸碱平衡对那碱度的那废水供应充分的缓冲量，当EGSB加工被用于处置TPD 废水，与污泥颗粒一起作用，EGSB反应器性能改善和变成更稳定。

命名原则

BOD5:五日生化需氧量,mg/L;SS:悬浮固体;COD:化学氧需求,mg/L;VFA:挥发性脂肪酸;COL:颜色;UFA:不饱和脂肪酸;EGSB:膨胀的颗粒状烂泥床;Vg:沼气生产率,m3/(公斤COD);HRT:水力保留时间,h;T:温度～6;K:电离常数;TA;MLSS,g/L;～ηCOD:化学需氧量除去;PV A:聚乙烯醇。

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[5 ]Monitoring and determination methods for water and wastewater [M] . 3rd. ed. Beijing : China Environmental Science Press.Guan B H , Wu ZB , Wu Z C et al . , 2003.1 .

[6 ]Gu X S , 19931 Mathematical model for wastewater bio-treatment [M] . 2nd ed. Beijing : Tsinghua University Press. Hulshoff P L , Lettinga G, 1986.1 .

[7 ]New technologies for anaerobic treatment [J ] . Water Science and Technology , 18 (2) : 41 631 Juragen H T , Wu WM, Mahendra KJ , 1990.1 .

[8 ]Ecoengineering high rate anaerobic digestion systems : Analysis of improved syntrophic biomethanation catalysts [J ] . Biotechnology and Bioengineering , 35 (10) : 990 6991 Kroeker E J , Schulte D D , Sparling A B et al . , 1979.1.

[9 ]Anaerobic treatment process stability[J ] . J Water Pollution Control Federation , 51 (4) :

718 67271 Leslie G C P , Henry C L , 1989.1 .

[10 ]Biological wastewater treatment : Theory and application(Li , X.W. , Yang , X. K. , Zhang , Y. G. ed. ) [M] . Beijing : China Architecture and Building Press. Souza M E , 1986.1.

[11 ]Criteria for the utilization , design and operation of UASB reactors[J ] . Water Science and Technology , 18 (12) : 55 661 Zhang X, Wang B Z , Zhu H , 1997.1.

[12 ]The Acid2alkaline equilibrium and buffer capacity of anaerobic digestion system[J ] . China Environmental Science , 17 (6) : 492 6951.

[13 ]Biodegradability of terephthalic acid in terylene artificial silk printing and dyeing wastewater [ J ] . Journal of Environmental Sciences , 15(3) : 296 6011.

Stability of expanded granular sludge bed process for terylene artificial silk printing and dyeing wastewater treatment

Abstract

Terylene artificial silk printing and dyeing wastewater (TPD wastewater), containing averaged 7.0 mg/L terephthalic acid (TA) as the main carbon source and the character pollutant, was subjected to expanded granular sludge bed (EGSB) process. The stability of the EGSB process was firstly conducted by laboratory experiment. TA ionization was the predominated factor influencing the acid-base balance of the system. High concentration of TA in wastewater resulted in sufficient buffering capacity to neutralize the volatile fatty acids (VFA)generated from substrate degradation and provided strong base for anaerobic system to resist the pH decrease below6.5. VFA and UFA caused almost no inhibition on the anaerobic process and biogas production except that pH was below 6.35 and VFA was at its maximum value. Along with the granulating of the activated sludge, the efficiency of organic removal and production rate of biogas increased gradually and became more stable. After start-up, the efficiency of COD removal increased to 57 %~64 %, pH stabilized in a range of 7.99 ~6.04, and production rate of biogas was relatively high and stable. Sludge granulating, suitable influent of pH and loading were responsible for the EGSB stability. The variation of VFA concentration only resulted inneglectable rebound of pH, and the inhibition from VFA could be ignored in EGSB. The EGSB reactor was stable for TPD wastewater treatment.

Keywords:expanded granular sludge bed; stability; anaerobic treatment; dyeing and printing wastewater Introduction：

In order to obtain pliable and elegant terylene fabric just like silk, terylene greige cloth is always pretreated with alkali-decomposition process, wherein terylene fiber is hydrolyzed to some extent in NaOH solution at certain temperature and pressure. During this process, the superficial terylene fibred is peeled off from the greige cloth and dissolved into solution, in which terylene acid (TA) and ethylene glycol are discharged as the main pollutants in

wastewater. The obtained terylene fabric with silken wrinkle and soft feeling is called artificial silk fabric. The alkali-decomposition of terylene can be described by the chemical equation below.

The wastewater from the alkali-decomposition process mixed with wastewater from printing, dyeing, potch and the other processes is named terylene artificial silk printing and dyeing wastewater ( T/D-wastewater ) . Only in Shaoxing County, East China, are there more than 300 thousands tons TPD-wastewater discharged each day.

Although the anoxic or aerobic bio-process has been the usual approach for the treatment of such kind of wastewater, various anaerobic process configurations were also found their usage in this field. However, the widespread application of anaerobic process has been hampered by the lack of understanding of factors associated with stability of the biological processes involved. The removal efficiency of organic substrates , the biogas production rate and the other items , which are involved in the stability of the process , depends on the acid-base balance. The characteristic pollutant TA in the TPD-wastewater is a kind of dual-organic acid , which exists in water in the form of molecule or ion state. It is still vague about the effect of TA to the acid-base balance in anaerobic system.

The expanded granular sludge bed ( EGSB) process developed from UASB process , is one of the controlled anaerobic treatment processes with advantages of higher rate and better toxic resistance. Although EGSB process has the efficiency of 27.1 % 68.0 % for chemical oxygen demand ( COD) removal and 31.4 % 66.0 % for TA removal

(Guan , 2003) , further development of EGSB technology for TPD-wastewater treatment depends upon a better understanding of the process stability. In this paper , the stability of the

process was discussed , the acid-base balance was emphasized and lab scale experiments were conducted.

1 Experimental

1.1 Wastewater and activated sludge

The wastewater in the experiment was taken from the central pump station for 3 605 t/d TPD wastewater in Shaoxing County , Zhejiang Province , China. After a one-year round survey , the main pollutants in the wastewater are given in Table 11 TPD wastewater characterized by high pH , COD value and color (COL) is different from traditional printing and dyeing wastewater. The value of COD varies from 780 mg/L to 3116 mg/L ; and biological oxygen demand for 5 d (BOD5 ) from 325 mg/L to 1436 mg/L. TA ranging from 286 Mg/L to 1279 mg/L is the characteristic pollutant controlling

40 % 68 % of the total COD in TPD wastewater. Activated sludge for the experiment was obtained from the treatment facility for pesticide wastewater , printing and dyeing wastewater and phenol wastewater. Sludge was acclimated firstly in a laboratory anaerobic reactor running in a fill and drawn mode under the same conditions as EGSB reactor to retain high concentration of biomass.

1.2 Experimental set-up and process

The columned EGSB reactor was divided into four compartments (Fig. 2) : (1) the granular sludge bed in which the granulated sludge was accumulated ; ( 2) the fluidized zone in which sludge was suspended ; (3) the gas-liquid- sludge separator ; and (4) the setting zone. The influent and reflux from the recycle pump was pumped into the bottom of the reactor and passed through the granular sludge bed.

Above the granular sludge bed , a fluidized zone developed mainly due to wastewater recycle. In the granular sludge bed and fluidized zone , the biological degradation took place and the biogas was produced. As mixed liquor passed through the gas-liquid-solid separator , the sludge with good setting abilities settled back through the apertures of the separator to the fluidized zone and sludge bed , while some flocculated and dispersed sludge was washed out

of the reactor with effluent , the effluent flowed into the storage vessel from the weir , and biogas flowed into a wet gas flow meter. The reactor ( Fig. 2) is 1.5 meter high with fluidized zone and sludge bed f100 6 , effective cubage of 7.0 L and a setting compartment of 2.0 L.

A schematic drawing of the experimental setup is shown in Fig. 31 In order to eliminate the inhibition from high pH and shortage of N and P , the feeding wastewater was first adjusted to the concentration of COD:N:P = 200:5:1 in wastewater reservoir by adding dipotassium hydrogen phosphate and ammonia sulfate and pH =10.0 by adding dilute hydrochloric acid in a neutralization reactor controlled by titrator. A pump was used to supply wastewater continuously to EGS

B reactor charged with mixed accumulated sludge capable of carbon degradation. Reaction temperature was controlled with a heater and a temperature controller.

The pH was monitored and adjusted with a titrator (DL55 , Mettler Toledo , Germany ) . Temperature was determined with a thermo probe connected to an infrared ray heater. Test of the other items was conducted according to the standard methods ( Editorial Board of Environment Protection Bureau of China , 1997) .

During the start-up of the EGSB reactor , phosphate and carbonate containing Ca , Fe , Al , Ni etc. were added into mixed liquor to enhance the granulating of the activated

sludge. The ratio of TPD wastewater in the influent was gradually increased to 100 %. The stability of the process was valued while start-up was conducted by increasing sludge loading and hydraulic loading step by step. During the EGSB reactor start-up , it was operated at influent pH 6.3 6.8 and hydraulic load 0.002 64 m3/(m3

d ) and up-flow linear velocity 0 —2.0 m/h , with temperatur

e controlled at 33 ℃(Table 2) . Generally , start-up stage for anaerobic process could be defined as the transitional stage before the reactor working steadily. The parameters indicating reactor performance during start-up include removal efficiencies o

f pollutants , biogas production rate , variation of pH , concentration of VFA and so on. After the EGSB reactor start-up , it was operated at a Flow-rate about 7.5 LPd and HRT 32 h in EGSB , 1 h in

neutralization reactor , while the hydraulic loading 22 609 m3/(m3 d) and up-flow linear velocity 1.0 6.0 m/h and temperature was controlled at 33 ℃( Table 2) . Stability of anaerobic reactor was valuated with COD removal efficiency , biogas production rate and pH value. All of these parameters involved in the stability depended on the acid-base balance in the reactor. So total-alkalinity , VFA and TA concentration were also tested.

1.3 Test and monitoring

Samples taken from mixed liquor were filtered immediately. Analysis of TA was carried on a high performance liquid chromatograph (HPLC , Gilson , France) . Aliquots of 25 ℃were injected to the HPLC , running with mobile phase of acetonitrile/water ( v/v) at 58/42 , and an addition of 2祃of concentrated H3 PO4 per liter of solution. The separation was performed using an ODS218 reversed phase column(Alltech , USA) at the flow-rate of 1.5 ml/min and column temperature of 25 ℃. An UV detector was used with the wavelength at 254 nm. It is measured that TA retention time was at 4.57 6.63 min.

2 Results

2.1 Sludge granulating and EGSB reactor start-up

The start-up is a process of sludge granulating that is essential for EGSB reactor (Hulshoff , 1986) . Start-up often takes 2 6 months , even as long as one year (Juragen , 1990) . The influent COD and TA were controlled at 1250 61943 mg/L and 563 6.41 mg/L , respectively. The hydraulic loading was adjusted to suit for sludge settling

back. Fig. 4 shows the sludge characteristics along the axis at the day 30 and the day 60 during reactor start-up. Activated sludge appeared to be heterogeneous distinctly along the axis of reactor , in which could be divided into sludge bed , sludge suspended zone and setting zone at the day 60.Granular sludge which diameter is over 1.0 mm occupied more than 10 % of total sludge in EGSB reactor at the day 60.

The substrate concentration along reactor axis is shown in Fig. 5. Above 0.4 m height , COD concentration at different height closed extremely to each other except in setting zone. From the bottom to 0.4 m axial height of the reactor , COD concentration stepped down extremely. The COL appeared the same as the COD. Removal efficiency of

COD increased from 23.6 % at the day 30 to 49.1 % at the day 60 , and the removal efficiency of COL increased from 60 % at the day 30 to 75.0 % at the day 60. The reactor performance changed with the sludge granulating. The EGSB reactor for TPD wastewater treatment started up normally. The biodegradation occurred chiefly in sludge bed , and the outside loop resulted in intensive mixing of wastewater in EGSB reactor.

2.2 Stability of the EGSB operation

Effluent pH , COD removal efficiency (ηCOD) and biogas production rate ( Vg , amount of biogas from 1 kg COD removal under standard state) were used to indicate the EGSB reactors performance. Fig. 6 shows the performance variation of EGSB during start-up period. From the day 10 to the day 28 , TPD wastewater in influent increased proportionally. The first peak value of ηCOD was presented between the day 15 and the day 20 , with Vg 0.11 6.18 m3/(kgCOD) . The efficiency of COD removal and the biogas production rate were much unstable , and decreased sharply when TPD wastewater in influent increased excessively. From the day 28 , influent was all of the TPD wastewater. Between the day 30 and the day 45 , effluent pH was 7.45 6.05 , ηCOD was 36 %69 % and Vg was 0.015 6.20 m3/( k gCOD) . The variation of effluent pH , ηCOD and Vg were remarkable before the day 45. It was a differentiation period for activated sludge.

After the day 45 , effluent pH stabilized in a range of 7.99 6.04 ,ηCOD increased to 57 %64 % , Vg also kept a stable value of 0.12 6.17 m3P( kgCOD) . In fact , from the day 45 , the granule sludge differentiated from sludge , and EGSB reactor presented its better stability. It was measured that granular sludge was made up of 10 % of the total sludge at the day 60. The sludge bed was charged with the 65 % of the total sludge while only took -5 % of the reactor cubage. EGSB reactor抯performance improved and became more stable along with the sludge granulating. It was noticeable that the efficiency of COD removal was always below 75 % because TA remained as slowly biodegradable substrate under anaerobic conditions with a turnover between 31.4 % and

56.0 %(Guan , 2003) . The EGSB reactor kept in halted state for 45 d at the temperature of 20 65 ℃after three months operation. Fig. 7 illustrates the reactor restart . The biogas production rate increased step by step. The COD removal was relatively stable with efficiency of 40 %60 %. The reactor restart only took 12 d. After maximum turnover rates of COD averaged 60 % , the system was switched to a load shocking with higher hydraulic load as much as 200 % of the normal load at the day 16. The depression of biogas production was in the wake of the shocking load. The COD removal efficiency decreased with a lag of several days after the anaerobic system received the shocking load. The results illustrated that the

performance of EGSB reactor could be unstable when the operation parameter changed greatly. The removal of COD recovered to a normal level of 55 %62 % in a week , while the biogas production recovered to the normal level of 0.11 60.15 m3/(kgCOD) in 10 d.

3 Theoretical calculation and discussions

3.1 Acid-base balance and buffering capability of TPDWastewater

The pH is one of the most important parameters indicating the stability of anaerobic system. The best pH for methanogenic bacteria is from 6.5 to 7.5 ( Souza , 1986) .

While VFA accumulating leads to a decrease of pH , the efficiency of the anaerobic treatment has already declined markedly ( Gu , 1993) . Therefore , it is more important to control VFA than to control pH in anaerobic system. The alkalinity is regarded as an important role to resist the VFA accumulation so as to increase pH in an anaerobic system

(Kroeker , 1979 ; Gu , 1993) . Alkalinity of the wastewater is defined as the gross substance which can react rationally with strong acids. Alkalinity includes many kinds of alkali components such as carbonates , bicarbonates , hydrates and organic base. They are called as total alkalinity in the wastewater (Editorial Board of Environment Protection Bureau of China , 1997) . The TPD wastewater has complex components and the concentration of carbonates , bicarbonates and hydrates cannot be obtained expediently. So the total alkalinity was used as a significant indicator for the basic components in the wastewater. Commonly , acid-base balance of the mixed liquor in anaerobic reactor is dominated by ionization balance of ammonia , VFA and carbonates (Kroeker E J , 1979 ; Zhang , 1997) .

Ammonia ionization equilibrium as Equation (2) :

NH3H2O=NH++ OH-. (2)

As the [ H+ ] increases , pH decreases and equilibrium shifts to the right . At 35 ℃, the ionization constant is 1.85 60-5

VFA is usually composed by acetic acid and propionic acid. As two kinds of VFA have close ionization constants , the ionization equilibrium can be simplified as the acetic acid

毕业设计外文翻译资料

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安全工程专业英语部分翻译

Unit 1 safety management system Accident causation models 事故致因理论 Safety management 安全管理Physical conditions 物质条件 Machine guarding 机械保护装置 House-keeping 工作场所管理 Top management 高层管理人员 Human errors 人因失误Accident-proneness models 事故倾向模型 Munitions factory 军工厂Causal factors 起因Risking taking 冒险行为Corporate culture 企业文化Loss prevention 损失预防Process industry 制造工业Hazard control 危险控制Intensive study 广泛研究Organizational performance 企业绩效 Mutual trust 相互信任Safety officer 安全官员 Safety committee 安全委员会Shop-floor 生产区Unionized company 集团公司Seniority 资历、工龄Local culture 当地文化 Absenteeism rate 缺勤率Power relations 权力关系Status review 状态审查 Lower-level management 低层管理者 Business performance 组织绩

效 Most senior executive 高级主管 Supervisory level 监督层Safety principle 安全规则Wall-board 公告栏Implement plan 执行计划Hazard identification 危险辨识 Safety performance 安全性能 One comprehensive definition for an organizational culture has been presented by Schein who has said the organizational culture is “a pattern of basic assumptions – invented, discovered, or developed by a given group as it learns to cope with its problems of external adaptation and internal integration –that has worked well enough to be considered valid and, therefore, to be taught to new members as the correct way to perceive, think, and feel in relation to those problems” 译文：Schein给出了组织文化的广泛定义，他认为组织文化是由若干基本假设组成的一种模式，这些假设是由某个特定团体在处理外部适应问题与内部整合问题的过程中发明、发现或完善的。由于以这种模式工作的有效性得到了认可，因此将它作为一种正确的方法传授给新成员，让他们以此来认识、思考和解决问题[指适应外部与整合内部的过程中的问题]。 The safety culture of an organization is the product of individual and group values, attitudes, perceptions, competencies, and patterns of behavior that determine the commitment to, and the style and proficiency of , an organization’s health and safety management. 译文：组织的安全文化由以下几项内容组成：个人和群体的价值观、态度、观念、能力和行为方式。这种行为方式决定了个人或团体对组织健康安全管理的责任，以及组织健康安全管理的形式和熟练程度。 Unit 2 System Safety Engineering System safety engineering 系统安全工程By-product 附带产生的结果

环境工程毕业设计开题报告范文

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如何变废为宝便成了节约用水的一项重要措施而炼油工业产生的废水成分又极为复杂故要想很好的处理炼油工业产生的废水并加以回用就谨慎严格的设计第二个就是毕业设计是本专业学生在完成全部课堂教学之后所进行的一项极为重要的实践性教学环节旨在通过具体的工程实践进一步深入理解、掌握和综合运用所学的专业理论知识进行污水处理设计基本技能的训练培养分析问题和解决问题的能力从而全面实现本专业学生的质量管理目标此次毕业设计的课题是"炼油工业废水处理技术与回用工艺设计" 本次设计进水为炼油工业废水处理水量为4.5×104m3/d 其进水水质参数如表1 进水中的浮油含量达10% 生物二级处理应达到《污水综合排放标准GB8978-1996》最终处理后的出水水质应达到《辽宁省地方标准DB 211627-2008》内容涉及到污水处理、处理水回用等各方面的专业知识以及应用计算机进行CAD绘图的实际应用能力在独立进行课题设计时将对本专业知识加深理解也将了解到环境工程专业在国内外的最新发展状况和技术的发展趋势表1 进水水质参数污水水质主要指标 CODcr （mg/L） BOD5 （mg/L） SS （mg/L）氨氮（mg/L） pH 温度（OC）设计污水水质 5500 1500 200 65 6-10 15-45

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外文资料名称： Design and performance evaluation of vacuum cleaners using cyclone technology 外文资料出处：Korean J. Chem. Eng., 23(6), (用外文写) 925-930 (2006) 附件： 1.外文资料翻译译文 2.外文原文

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环境工程专业毕业设计要求主考：河海大学一、毕业设计要求、综合运用所学的基本理论、基本知识和基本技能，联系工作实际进行选题，选题后按任务书要求进行设计。、有一定的应用性和科学性，文笔流畅，表达清晰。、毕业设计提纲、初稿、完成稿均需纸打印。、以下为参考选题，也可自己选题。二、做环评毕业论文的答辩要求：（）各自准备好分钟的，介绍所做论文的主要内容（图文并茂），特别是自己独立完成的部分，重点部分（评级等级确定、工程分析、现状评价、预测评价等）要求介绍具体过程，不能一带而过（答辩的好坏计入成绩）；（）介绍完后由答辩老师提问，学生回答问题，分钟左右；（）可以自带参考材料，但不能频繁翻阅，对自己做的主体内容必须熟练，并能迅速回答相关问题，答辩老师的提问主要是基于你们做的论文，但不限于此；

三、做工程设计论文的答辩要求：（）各自准备好分钟的，介绍所做论文的主要内容（图文并茂），特别是自己独立完成的部分，重点介绍（工程规模、来水水质、处理目标、执行标准、处理工艺比选、工程投资、平面高程布置等）要求介绍具体过程，不能一带而过（答辩的好坏计入成绩）；（）介绍完后由答辩老师提问，学生回答问题，～分钟左右；（）可以自带参考材料，但不能频繁翻阅，对自己做的主体内容必须熟练，并能迅速回答相关问题（）答辩过程中的提问主要是基于设计的内容、步骤、要求，并会涉及主要构筑物工作的基本原理，但不限于此；环境工程专业毕业设计参考选题环境影响评价毕业设计任务书（一）毕业设计题目某水厂工程项目环境影响评价毕业设计目的

综合运用所学的基本理论、基本知识和基本技能，对某水厂工程项目进行环境影响评价，分析解决实际问题，进行工程师所必需的综合训练，在不同程度上提高研究、查阅文件、进行环境影响评价的能力。三、毕业设计任务根据环境影响评价导则等相关要求进行某水厂工程项目环境影响评价，具体内容有：、环境质量现状评价；、环境影响预测评价；、污染防治措施；、环境风险分析；、总量控制；、公众参与等。四、毕业设计成果、环境影响报告书、就环境影响评价中遇到的一个问题进行讨论，并必要的讨论。五、原始资料选题后通过向指导教师索取。环境影响评价毕业设计任务书（二）毕业设计题目某污水处理工程项目环境影响评价毕业设计目的综合运用所学的基本理论、基本知识和基本技

环境工程毕业设计摘要前言

摘要克什克腾旗经棚镇位于赤峰市西北部，大兴安岭山脉与阴山山脉交汇处，镇区周边条件较多，三面环山，两水汇一，镇区生活区向北发展，工业区字山以南发展。当地水资源紧缺，污水的处理和再利用问题已经迫在眉睫。本次毕业设计的题目为克什克腾旗经棚镇污水处理厂工程设计。主要任务是工艺流程选择及构筑物设计和计算。该污水处理厂工程设计规模两万吨/日，采用A/O工艺。该工艺具有出水水质稳定，除磷效果好，进水为连续流，对温度适宜性强。抗冲击负荷能力强等特点该污水厂的污水处理流程为:从泵房提升到格栅流入沉砂池，进入A/O池，二沉池，最后出水;污泥的流程为：从二沉池排出的剩余污泥进入污泥浓缩脱水一体机，进一步脱水后，污泥外运。

Abstract KeShenKeTengQi tent town is located in the northwest of chifeng city, the greater hinggan mountains and the yinshan mountains, township surrounding conditions more, surrounded on three sides by mountains and faces the two water transfer, township development living areas to the north, industrial word mountains south of development. Local water resources, sewage treatment and reuse problem is imminent. The graduation design topic for KeShenKeTengQi tent town sewage treatment plant project design. Main task is to process selection and structure design and calculation. The scale of twenty thousand tons/day sewage treatment plant engineering design, adopting A/O process. This process has the effluent is stable, the phosphorus removal effect is good, water as the continuous flow, the temperature suitability is strong. Strong ability to resist impact load characteristics The sewage plant of wastewater treatment process for: from pump house to the grating into the grit chamber, into the pool of A/O, and the second pond, finally out of the water; Sludge process for: from the second pond, the surplus sludge discharge into the sludge concentration and dehydration machine, after further dehydration sludge sinotrans. 关键词：污水处理 A/O工艺污泥浓缩 Key words: Sewage treatment sludge concentration of A/O process