【正文】 (3) no primary and secondary settles。 Formate1. IntroductionIn China, there are more than 100 big breweries in which a great volume of wastewater is produced. For each cubic meter of beer produced, the water consumed in general is 10~20m3, of which more than 90% will be discharged into sewer system. Moreover, there exists a great amount of beer losses (~%) in production line, which is also entering wastewater collecting system finally. Because of the high biodegradability of brewery wastewater (BOD5/COD), biological treatment is widely used. Traditionally, wastewaters from different processes are mixed together and treated with aerobic processes, such as conventional activated sludge, oxidation ditch, sequencing batch reactor and biofilter. However, brewery wastewater is characterized by high strength soluble organic pollutants and suspended solids (SS). Aerobic treatment requires an intensive amount of energy for aeration. In addition, a large amount of wasted sludge is produced, which costs large capital to disposal. Therefore, Brewery panies are reluctant to employ wastewater treatment facilities. Source separation is an alternative for sustainable solution. For the part of wastewaters discharged from boiling and fermentation processes in which high strength organic carbon is contained, anaerobic treatment is believed to be the best choice. High rate anaerobic reactors, such as upflow anaerobic blanket reactor (UASB), anaerobic granular bed baffled reactor (GRABBR) and anaerobic fluidized bed (AFB), have been reported to treat brewery wastewater and a satisfactory COD reduction obtained.Anaerobic sequencing batch reactor (ASBR) is a newly developed technology and has been extensively studied due to its advantages: (1) no short circuit, as in the case of fixedbed continuous systems。 Granular sludge。表231 沿程水損表管渠構(gòu)筑物名稱管徑DNmm管長m管道水損m局部水損m合計m集水池—粗格柵5002管渠構(gòu)筑物名稱管徑DNmm管長m管道水損m局部水損m合計m細格柵—調(diào)節(jié)池50010調(diào)節(jié)池—UASB反應器50014UASB反應器—生物接觸氧化池50014生物接觸氧化池—沉淀池50030沉淀池—消毒池50012消毒間—排水口5000（1）各構(gòu)筑物自身水損取值如下表：232 各構(gòu)筑物自身水損構(gòu)筑物構(gòu)筑物自身水損（m）構(gòu)筑物構(gòu)筑物自身水損（m）細格柵提升泵房粗格柵調(diào)節(jié)池UASB反應器生物接觸氧化池沉淀池消毒間（2）根據(jù)表231和表232確定各構(gòu)筑物高程如下表：表233 廢水處理站各構(gòu)筑物高程編號管渠及構(gòu)筑物名稱水面上游標高（m）水面下游標高（m）構(gòu)筑物水面標高（m）超高(m)池底標高（m）池頂標高(m)1集水池3132粗格柵13提升泵4細格柵5調(diào)節(jié)池16UASB反應器編號管渠及構(gòu)筑物名稱水面上游標高（m）水面下游標高（m）構(gòu)筑物水面標高（m）超高(m)池底標高（m）池頂標高(m)7生物接觸氧化池8沉淀池9消毒池附錄附錄一 英文翻譯英文原文Treatment of brewery wastewater using anaerobic sequencing batch reactor (ASBR)Shao Xiangwen *, Peng Dangcong, Teng Zhaohua, Ju XinghuaSchool of Environmental and Municipal Engineering, Xi’an University of Architecture and Technology, Xi’an 710055, ChinaAbstractBrewery wastewater was treated in a pilotscale anaerobic sequencing batch reactor (ASBR) in which a floating cover was time experiments showed that the reactor worked stably and effectively for COD removal and gas production. When the organic loading rate was controlled between , and hydraulic retention time one day, COD removal efficiency could reach more than 90%. Sludge granulation was achieved in the reactor in approximately 60 days, which is much less than the granulation time ever reported. In addition, high specific methanogenic activity (SMA) for formate was observed. The study suggests that the ASBR technology is a potential alternative for brewery wastewater treatment.Keywords: Brewery wastewater。（2）彎管和閥門等的局部水頭損失 （式33）式中：—局部阻力系數(shù)； ν—流速，m/s； g—重力加速度。（1） 沿程管道水損 （式31）式中：i—水力坡度； l—管道長度，m。（1）總污泥流量（2）脫水后污泥量選用一臺DYL—2000型帶式壓濾機。設池底坡度為i=，則池底坡降故池底可貯泥容積式中：R—濃縮池半徑，m。d）。UASB反應器產(chǎn)生污泥：Q1=，含水率P1=98%；沉淀池產(chǎn)生污泥：Q2=210m3/d，含水率P2=98%；停留時間：T=24h；濃縮池個數(shù)n=2。（3）總污泥量選用50XG—C—230型固液泵兩臺，其中一臺備用。沉淀池進水懸浮物濃度：C1=；沉淀池出水懸浮物濃度：C2=。加氯量：選用MJL—Ⅰ型加氯機，該型號加氯機規(guī)格及性能：（1）加氯量：~；（2）使用水壓力：~；（3）外形尺寸（長高）：180mm305mm；（4）重量：7kg。（9） 沉淀池總高度式中：h1—超高，m，； h4—緩沖層高，m。（7） 沉淀部分有效容積 式中：C1—進水懸浮物濃度，t/m3，104t/m3； C2—出水懸浮物濃度，t/m3；取值7105t/m3； T—兩次污泥清除相隔時間，d，取值2d； γ—污泥密度，t/m3，取值1； P0—污泥含水率，%，取值98。（4） 沉淀部分有效段面積式中：K2—水流量總變化系數(shù)，取值1； ν—污水在沉淀池中流速，m/s。設計流量Q=15000m3/d=625m3/h=；中心管內(nèi)流速ν0=20mm/s；（1） 中心管面積采用4個豎流式沉淀池，則每個沉淀池流量為則中心管面積為式中：qmax—每池最大設計流量，m3/s； ν0—中心管內(nèi)流速，m/s。（6）廢水在池內(nèi)實際停留時間（7）所需填料總體積（8）需氣量式中：D0—每立方米污水需氣量，m3/m3，取值15m3/m3。（2）氧化池總面積式中：H—填料層總高度，m。設計流量Q=15000m3/d=625m3/h=；進水BOD5濃度La=220mg/L；出水BOD5濃度Lt=20mg/L；容積負荷M=1800gBOD/(m3?d)；填料層總高度H=3m；填料層數(shù)m=3。③ 氣水分離器氣水分離器起到對沼氣干燥的作用，選用Φ500mmH2000mm鋼制氣水分離器一個，氣水分離器中預裝鋼絲填料，在氣水分離器前設置過濾器以凈化沼氣，在分離器出氣管上裝設流量計及壓力表。水封高度式中：H1—集氣室氣液界面至沉降區(qū)上液面的高度，取值2m； H0—反應器至貯氣罐的壓頭損失和貯氣罐內(nèi)的壓頭。（6）沼氣收集系統(tǒng)設計① 沼氣總產(chǎn)氣量計算式中：r0—設計產(chǎn)氣率取，m3/kg COD。據(jù)VSS/SS=，② 單池產(chǎn)泥量③ 總污泥產(chǎn)量式中：ρs—污泥密度，kg/m3，取取值1000kg/m3； P—污泥含水率，%，取值98%。② 每個布水點服務面積（4）出水系統(tǒng)的設計出水系統(tǒng)采用鋸齒形出水槽出水，每個反應器共設兩條出水槽。在每個UASB反應器底部沿池長均勻設置8條平行管道，每條管道上均勻設置16個布水點，進水方式采用連續(xù)進水。⑩ 校核（3）進水系統(tǒng)設計UASB反應器的進水系統(tǒng)是很關(guān)鍵的一部分，它對于形成污泥和進水間的充分接觸，最大限度的利用反應器內(nèi)的污泥是十分重要的。④ 上下三角形集氣罩之間回流逢中流速式中：b3—上三角集氣罩與下三角集氣罩的水平距離，m。圖212 三相分離器結(jié)構(gòu)示意圖① 下三角集氣罩底水平寬度式中：h3—下三角集氣罩的垂直高度，m，取值1m； ɑ—下三角集氣罩的垂直高度，取值55176。設上下三角形集氣罩斜面水平夾角α=55176。本工程設計中，與短邊平行，沿長邊每池布置13個集氣室，構(gòu)成13個分離單元，則每池設置13個三相分離器。③ 沉淀槽斜底與水平面的夾角不應小于50176。根據(jù)已有經(jīng)驗，三相分離器應滿足以下幾點要求：① 混合液進入沉淀區(qū)之前，必須將其中的氣泡予以脫除，防止起泡進入沉淀區(qū)影響沉淀。② 分離并收集厭氧消化所產(chǎn)生的氣體。則池長L=26m，池寬B=13m。② 反應器總表面積式中：H—反應器有效高度，m。 UASB反應器設計流量Q=15000m3/d=625m3/h=；有機物容積負荷q=5kgCOD/(m3?d)；反應器有效高度H=4m；采用四座矩形UASB反應器。設計流量Q=15000m3/d=625m3/h；調(diào)節(jié)池設計停留時間T=。細格柵選用1臺TGS—1000型回轉(zhuǎn)式格柵（齒耙）除污機。（6）柵前槽高式中：h1—柵前渠道超高，m。（2）柵槽寬度（取B=）（3）進水渠道漸寬部分長度式中：B1—進水渠道寬度，m，；