31中英文雙語外文文獻翻譯成品利用正向滲透應(yīng)用于廢活性污泥同步增稠、消化和直接脫水的可行性

1、<p>　　外文標題：Feasibility of applying forward osmosis to the simultaneous thickening, digestion, and direct dewatering of waste activated sludge</p><p>　　外文作者：Hongtao Zhu , Liqiu Zhang , Xianghua Wen , Xia

2、 Huang</p><p>　　文獻出處:《Bioresource Technology》 , 2012 , 113 (113) :207-213</p><p>　　英文5098單詞， 26874字符，中文7485漢字。</p><p>　　此文檔是外文翻譯成品，無需調(diào)整復(fù)雜的格式哦！下載之后直接可用，方便快捷！只需二十多元。</p><p&

3、gt;　　Feasibility of applying forward osmosis to the simultaneous thickening, digestion, and direct dewatering of waste activated sludge</p><p>　　Hongtao Zhu , Liqiu Zhang , Xianghua Wen , Xia Huang</p>

4、<p><b>　　Abstract</b></p><p>　　The feasibility of applying forward osmosis (FO) to the simultaneous thickening, digestion, and dewatering of waste activated sludge w as investigated. After

5、 19 days of operation, the total reduction in efficacy of the instantaneous sludge thickening and digestion system in term of mixed liquid suspended solids (MLSS) and mixed liquid volatile suspended solids (MLVSS) was ap

6、proximated at 63.7% and 80% , respectively, and the MLVSS / MLSS ratio decreased from 80.8% to 67.2%. The MLSS concentratio</p><p><b>　　Keywords:</b></p><p>　　Forward osmosis, Waste

7、activated sludge, Sludge thickening, Sludge dewatering, Aerobic digestion </p><p>　　1. Introduction</p><p>　　Large quantities of excess high water content are produced in wastewater treatment

8、plants (WWTPs) everyday. To minim the costs of sludge transportation and handling, reduction in sludge volume and through water separation is the most important that needs to be addressed prior to final disposal. Sludge

9、thickening and dewatering are usually practiced for volume and reduction. Normally, sludge thickening is performed to reduce the sludge volume and increase the sludge solid content to obtain a suit</p><p>　　

10、To solve the problem s of conventional sludge thickening technologies and shorten the sludge treatment processes (i.e., to lessen the footprint and operational strength), a ?atsheet membrane was developed for simultaneou

11、s sludge thickening and digestion process (Wang et al., 2008a). This sludge reduction system is actually a membrane bioreactor (MBR), whose advantages include a small footprint, high pollutant removal ef?ciency, and low

12、cost for the retreatment of the thickened supernate, among o</p><p>　　In contrast to conventional MBR, several researchers proved that a forward osmotic MBR has better membrane fouling control performance (C

13、ornelissen et al., 2008; Lay et al., 2011; Achilli et al., 2009b). In forward osmosis (FO), such as in the well-known reverse osmosis (RO), water is transported across a semipermeable membrane, which is impermeable to sa

14、lt and is driven by the difference between the osmotic pressures across the membrane (Cath et al., 2006). Even though osmosis has been recogniz</p><p>　　In FO, the reconcentration of the draw solution (DS),

15、usually com posed of dissolved salts, is a major part of the energy consumption. The current study proposes the utilization of RO concentrates in seawater desalination as the DS. In RO, typical seawater recoveries are be

16、tween 30% and 50% (Ji et al., 2010; McCutcheon et al., 2005). Discharge of the concentrated brine back into the sea is proven to affect marine fauna and ?ora (Latorre, 2005) and dam ages benthic organism s due to the coa

17、gulant</p><p>　　In the current study, FO was innovatively applied to simultaneous thickening, digestion, and direct dewatering of raw waste activated sludge from WWTPs. The DS was synthesized to simulate the

18、 concentrated brine of seawater desalination RO (Ji et al., 2010) and was not reconcentrated to minimize the energy demand. The current work aims to conduct a preliminary study on the characteristics (including the diges

19、tion ef?ciency, the reversed salt transport, and the effects of DS concentration on the F</p><p><b>　　2.Methods</b></p><p>　　2.1. Experimental setup and the FO membrane</p>&l

20、t;p>　　The bench-scale FO experimental setups for simultaneous sludge thickening, digestion, and dewatering are shown in Fig. 1. In the sludge thickening and digestion system , the single FO membrane module unit consis

21、ted of two plexiglass cells that clipped the FO membrane sheet. The effective membrane surface area of a single unit was approximately 0.0133 m 2. Depending on the ?ux requirements, one to three membrane modules can be u

22、sed for one reactor. The reactor had a cylindrical con?guration and a</p><p>　　The membrane module used in the sludge dewatering system was similar to a ‘‘sandwich’’. The circulation pump pushed the DS throu

23、gh the airtight channel, the bottom layer of the ‘‘sandwich’’. The middle layer was the FO membrane, and the top layer was a sludge container. Both the DS and the sludge were in direct contact with the FO membrane. The e

24、ffective membrane area of this module was approximately 0.0035 m 2,and the sludge container had a length of 7 cm , a width of 5 cm , and a maxim um dept</p><p>　　The FO membrane used in the study was supplie

25、d by Hydration Technology (HTI, Albany, Oregon, US) and classi?ed as cartridge type. The 50 l m -thick FO membrane was made of cellulose triacetate embedded in a polyester screen mesh (Cath et al., 2006). The HTI membran

26、es, which have been used in a number of studies, are currently viewed as the best available membranes for FO applications (Achilli et al., 2009b; Lay et al., 2011;Holloway et al., 2007; Cornelissen et al.,2008; Xiao et a

27、l.,2011). The m</p><p>　　2.2. DS and activated sludge</p><p>　　As previously stated, synthetic DS # 1 was prepared to simulate the concentrated brine from RO (30%recovery rate) by dissolving(799

28、6 m g/L), NaHCO3 (274 m g/L), and Na2SO4 (4526 m g/L) in ultrapure water. For future applications, the RO concentrate can be discharged into the sea after dilution, similar to natural seawater. Synthetic DS # 5 was also

29、used in the tests and was prepared to simulate natural seawater by dissolving reagent grade NaCl 25,053 m g/L), CaCl2 2H2O (1608 m g/L), MgCl2 (5597 </p><p>　　The activated sludge was obtained daily from a 6

30、0,000 m 3/d MBR facility in a WWTP located in the northern part of Beijing. The sludge samples had a MLSS of 7.3 g/L, a MLVSS of 5.9 g/L, a soluble COD in supernatant of 103 m g/L, and a conductivity of 310 l S/cm .</

31、p><p>　　2.3. Analytical methods</p><p>　　Analyses of the mixed liquor suspended solids (MLSS), mixed liquor volatile suspended solids (MLVSS), chemical oxygen demand (COD), ammonia nitrogen, and to

32、tal phosphate were perform ed based on the standard methods proposed by the State Environ- mental Protection Administration of China. The soluble COD (SCOD) samples were prepared using ?lter papers with a nominal pore si

33、ze of 0.45 l m . The dissolved oxygen (DO) concentration was determined using a DO meter (Model YSI 58, YSI Research Incorpo</p><p>　　3. Results and discussion</p><p>　　3.1. Variations in the sl

34、udge concentration and digestion efficiency</p><p>　　The DO in the reactor was maintained at around 2.0 mg/L and the hydraulic retention time was about 1 day. During the experi-ments, the fluctuation in the

35、room temperature during daytime was 22–29 LC. The feed sludge volume for each day depended on the average FO membrane flux of that day. The concentration of the feed sludge also varied, depending on the operation of the

36、MBR facility. No sludge was withdrawn during the experiments.</p><p>　　The variations in MLSS and MLVSS and, consequently, the MLSS/ MLVSS ratio with the operation time are shown in Fig. 2(a). Both the MLSS

37、and MLVSS concentrations showed increasing trends be-cause of the FO thickening process and the absence of sludge dis-charge. The quantity of pure water extracted from the FO thickening process was calculated and will be

38、 discussed in the next section. In the 19 days of operation, the MLSS and MLVSS concentrations quickly increased during the first 7 days and gra</p><p>　　The total reduction efficiency values of MLSS and MLV

39、SS were approximately 63.7% and 80%, respectively [Fig. 2(b)]. The MLSS reduction efficiency is comparable to the results of Kim et al. (2010), where they achieved an MLSS destruction efficiency rate of 60% using a subme

40、rged MBR. However, the obtained MLSS reduction efficiency was lower than that of another submerged MBR sludge thickening system used by Wang et al. (2008a), where the latter achieved an MLSS digestion efficiency of about

41、 80% in</p><p>　　3.2. Membrane flux decline and reversed salt transport during sludge thickening</p><p>　　The aerobic digestion and sludge thickening simultaneously occurred. Based on the MLSS c

42、oncentration of 39 g/L and total MLSS digestion rate of 63.7% on the 19th day, the final calculated MLSS without sludge digestion was approximately 107 g/L. Thus, through the FO sludge thickening system, the activated sl

43、udge can be thickened from a water content of 99.3% to approximately 90%, higher than that of most conventional sludge thickening processes.</p><p>　　The water ?ux under different DS concentrations as a func

44、tion of operating time is shown in Fig. 3(a). The ?ux evolution curves of DSs # 1, # 2, and # 3 share similar trends, with a rapid decrease at the beginning followed by a smooth development. This phenomenon shows that CP

45、 as well as a possible membrane fouling, rapidly occurred within the ?rst several days. Based on the variations in the relative ?ux over time [Fig. 3(b)], the ?ux reduction range of each test [Fig. 3(a)] decreased from D

46、S #</p><p>　　The ?ux reductions due to changes in the AOPD are shown in Fig. 4(b). Com pared with membrane fouling, the decrease in AOPD signi?cantly contributed to the ?ux reduction, indicating a dominant p

47、osition. AOPD decreased with DS concentration (i.e., from DS # 1 to DS # 5); this result is similar to the fouling trends. For each test, AOPD quickly developed during the ?rst5 days, then slowed in the next 10 days. Obv

48、iously, the AOPD development rate gradually decreased with operating time, similar to </p><p>　　FO membranes can reject most ions. However, some of the DS salts were able to pass through the FO membranes int

49、o the feed solution; this phenomenon is called salt leakage. This reverse- transported salt from the DS not only causes a reduction in the AOPD but also exhibits inhibitory or toxic effects on the m icrobial com m unity

50、inside the digestion reactor (Achilli et al., 2009a,b). The variation curves of the equivalent salt (NaCl) concentrations in the reactor are shown in Fig. 5. Although th</p><p>　　3.3. Characteristics of the

51、sludge dewatering FO process</p><p>　　In most presently used sludge dewatering methods, chemical or organic ?occulants are used to condition the sludge to facilitate dewatering. These additives increase the

52、cost of the process and tend to make the ?nal disposal of the sludge more dif?cult. For example, if the dewatered sludge is to be incinerated, the added chemicals may cause harmful effects during the incineration process

53、 and to the incinerator itself (Pugsley and Cheng, 1981). There- fore, in the current study, raw activated slud</p><p>　　The sludge dewatering performances of FO under different sludge depths and DS concentr

54、ations are shown in Fig. 6. Pugsley and Cheng (1981) reported that sludge depth has a signi?cant effect on dewatering ef?ciency. In their study, a 0.15%NaCl solution was used to simulate sludge to determine the effects o

55、f the sludge depth. The 0.15%NaCl solution does not accurately represent a real sludge because it can m ore easily maintain a constant water concentration com pared with real sludge when water o</p><p>　　The

56、 effects of DS concentration on the membrane ?ux, ?nal dry sludge content, and corresponding dewatering time are shown in Fig. 6(c) and (d). Not surprisingly, a higher DS concentration means higher ?ux, higher ?nal dry s

57、ludge content, and shorter corresponding dewatering time. However, a signi?cant sludge dewatering performance can also be achieved when seawater is used as the DS. Therefore, the use of seawater RO concentrates as the DS

58、 is feasible. In other words, even though DS # 5 showed t</p><p>　　Furthermore, FO was proven useful in sludge dewatering even without sludge thickening or chemical additives. Taking the use of seawater RO c

59、oncentrate as the DS into account, this design appears to have a low energy demand and is worthy of further investigation.</p><p>　　Conclusion s</p><p>　　The results of 19 days of operation usin

60、g the forward osmosis simultaneous sludge thickening and digestion system are presented. (1) The total reduction ef?ciency values of MLSS and MLVSS were approximately 63.7% and 80%, respectively. (2) The MLVSS/ MLSS rati

61、o decreased from 80.8%to 67.2%. (3) The MLSS concentration increased to 39 g/L from the initial concentration of about 7 g/L. The ?ux was primarily reduced due to the decrease of apparent osmotic pressure difference. Unl

62、ike traditional memb</p><p>　　Acknowledgements</p><p>　　The study is ?nancially supported by Beijing Forestry University Young Scientist Fund (BLX2009020) and special fund of State Key Joint Lab

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90、 Pollution Control. Higher Education Press Beijing.</p><p>　　利用正向滲透應(yīng)用于廢活性污泥同步增稠、消化和直接脫水的可行性</p><p>　　Hongtao Zhu , Liqiu Zhang , Xianghua Wen , Xia Huang</p><p><b>　　摘要</b&

91、gt;</p><p>　　本文中，對利用正向滲透（FO）應(yīng)用于廢水活性污泥同步增稠、消化和脫水的可行性進行了研究。在混合液體懸浮固體（MLSS）和混合液體揮發(fā)性懸浮固體（MLVSS）中運行19天后其瞬時污泥增稠和消化系統(tǒng)的效力分別近似降低63.7％和80％， MLVSS / MLSS比率從80.8％降至67.2％。 MLSS濃度從7g / L開始就達到39g / L，這表明其具有良好的增稠效果。 在使用正向滲透

92、FO進行污泥脫水時，考察了兩個主要因素，即初始污泥深度和汲取溶液（DS）濃度。 在將來的應(yīng)用中，推薦應(yīng)用3毫米的污泥深度，在大約1小時后，干污泥含量可達到約35％。 而且，本次研究印證了使用海水反滲透濃縮物作為DS的可行性。</p><p><b>　　關(guān)鍵詞：</b></p><p>　　正向滲透（FO）、廢活性污泥、污泥增稠、污泥脫水，好氧消化</p>

93、<p><b>　　引言</b></p><p>　　在污水處理廠（WWTP）每天都會產(chǎn)生大量有過量物質(zhì)的水。為了降低污泥運輸和處理成本，減少污泥量和通過水分離是最后一道處置程序之前需要解決的最重要的問題。污泥濃縮和脫水通常用于將體積減少。通常情況下，污泥濃縮的目的是為了縮小污泥的體積并增加污泥的固體含量，從而在污泥脫水過程中獲得適當濃縮的污泥。普遍使用的污泥濃縮過程包括重力稠

94、化、溶氣氣浮稠化和離心增稠等。盡管這些傳統(tǒng)的增稠技術(shù)已經(jīng)可以隨時使用，而且易于操作，但它們的應(yīng)用仍然存在很多問題。例如，重力增稠過程具有占地面積大、增稠效果低下的特點，在長期保存（SRT）期間有釋放磷的趨勢和發(fā)出令人不快的氣味的缺點（Wang等人，2008a; Kim等人。，2010）。另一方面，污泥消化處理是標準化操作，特別是對于大中型污水處理廠而言，在稠化過程之后，要采用穩(wěn)定化步驟以實現(xiàn)污泥穩(wěn)定、毒解和最小化（Wang等人。，200

95、8a）。除增稠和消化外，污泥脫水率約為70％。然而，目前污泥脫水仍然是成本最大和最不被了解的廢水處理工藝（Pei 等人2010，Yuan等人，2011）。 </p><p>　　為了解決傳統(tǒng)污泥濃縮技術(shù)存在的問題，簡化污泥處理工藝（即減少占地面積和降低運行強度），開發(fā)了一種同時用于污泥濃縮和消解過程的平板膜（Wang 等人，2008a）。 這種污泥減量系統(tǒng)實際上是一種膜生物反應(yīng)器（MBR），其優(yōu)點包括占地面積小

96、、污染物去除效率高以及對增稠上清液進行再處理的成本低（Judd，2006）。 盡管如此，相對較高的能量需求，尤其是由于高污泥濃度導(dǎo)致的膜污染，是膜污泥增稠工藝應(yīng)用的主要障礙（Wang 等人2008b，2009）。</p><p>　　與傳統(tǒng)的膜生物反應(yīng)器MBR相比，一些研究人員已經(jīng)證實正向滲透的膜生物反應(yīng)器MBR具有更好的膜污染控制性能（Cornelissen等，2008; Lay等，2011; Achilli等

97、，2009b）。在正向滲透（FO）中，例如在眾所周知的反滲透（RO）中，水被輸送穿過半滲透性膜，其對鹽不具滲透性，并且由跨過膜的滲透壓之間的間隙來驅(qū)動（Cath等人。，2006）。盡管人們已經(jīng)認識了其滲透性能且被利用了數(shù)十年，但FO仍然是一種獨特的新興技術(shù)（Chung等，2010）。在過去的幾年里，由于可獲得更高效的FO膜，已經(jīng)在FO研究上也作出了越來越大的努力（Cornelissen等，2008）。目前的FO應(yīng)用已經(jīng)從水處理和食品加工

98、擴展到發(fā)電和控制藥物釋放等新的方法之中（Wallace等，2008; Garcia-Castello和McCutcheon，2011; Achilli等，2009a Sotthivirat等，2007 ）。然而，在過去的30年中，還沒有關(guān)于在污泥增稠、消化和脫水中直接使用FO的研究。唯一相關(guān)的創(chuàng)造性研究是由Pugsley和Cheng（1981）在30多年前完成的。他們的研究主</p><p>　　在FO中，通常情

99、況下提取液（DS）的再濃縮組成了溶解鹽，是能量消耗的重要組成部分。目前的研究提出在海水淡化中使用RO濃縮物作為DS。在RO中，常見的海水回收率在30％到50％之間（Ji等人，2010; McCutcheon等人，2005）。由于鹽水中存在凝結(jié)劑（Lattemann和Höpner，2008），將濃縮的鹽水排入海中已被證實會影響海洋動物和浮游植物（Latorre，2005）和大壩底棲生物。這種現(xiàn)象對海水淡化RO而言，是一個重要的環(huán)