2010年11月農(nóng)業(yè)機(jī)械學(xué)報(bào)第41卷第11期DOI: 10.3969/j. isn.1000-1298. 2010.11. 018基于Fluent的固定床生物質(zhì)氣化爐冷態(tài)壓力場(chǎng)研究*孫宏宇'董玉平’周淑霞'董磊2景元琢”(1.山東大學(xué)高效潔凈機(jī)械制造教育部重點(diǎn)實(shí)驗(yàn)室，濟(jì)南250061;2.濟(jì)南百川同創(chuàng)實(shí)業(yè)有限公司,濟(jì)南250101)[摘要]以下吸式固定床生物質(zhì)氣化爐物理模型為研究對(duì)象,應(yīng)用流體仿真軟件Fluent,對(duì)冷態(tài)氣化爐在單、雙層氣化劑配風(fēng)工況下的床層壓力場(chǎng)進(jìn)行仿真研究。通過(guò)氣化爐多點(diǎn)測(cè)壓實(shí)驗(yàn),對(duì)仿真結(jié)果進(jìn)行驗(yàn)證。利用歐拉-拉格朗日方法分析氣化爐冷態(tài)流場(chǎng)分布特性,根據(jù)伯努利方程說(shuō)明氣化爐床層壓力場(chǎng)的變化原因。結(jié)果表明,仿真與實(shí)驗(yàn)結(jié)果的誤差值在2.5%以內(nèi),氣化劑配風(fēng)工況的變化改變了爐內(nèi)流場(chǎng),雙層氣化劑配風(fēng)使氧化層壓力場(chǎng)平均值為14.98kPa,高于單層配風(fēng)工況.且軸向壓力分布均勻。關(guān)鍵詞:生物質(zhì)氣化下吸式氣化爐 數(shù)值模擬 氣化壓力中圖分類號(hào): TK6文獻(xiàn)標(biāo)識(shí)碼: A文章編號(hào): 1000-1298(2010)11 0094-04Analysis of Fixed-bed Biomass Gasifier Cold InternalPressure Field Based on FluentSun Hongyu' Dong Yuping'Zhou Shuxia' Dong Lei? Jing Yuanzhuo2(1. Key Laboratory of High Efficiency and Clean Mechanical Manufacure，Ministry of Education, Shandong University ,Ji'nan 250061, China 2. Ji'nan Baichuan Tongchuang Company lsd. , Ji'nan 250101, China)AbstractTaking the physical model of downdraft biomass gasifier as the research object, fluid simulationsoftware Fluent was used, the pressure field of the gasifier that in the condition of single-layer air-distribution and double-layer air-distribution was comparatively analyzed. By means of multi-pointpressure measurement experiment, the simulation results were verified. The Euler - Lagrange model wasused to analyze the cold characteristics flow field distribution of gasification. The reason of diversificationin pressure field by Bernoulli's equation was discussed. The results showed that the deviation value ofsimulation and experimental results was under 2. 5% . Different air-distribution condition should lead tothe changes of flow field in biomass gasifier. Double-layer air-distribution condition made the averagepressure in oxidation area of 14. 98 kPa, higher than that in the condition of single air distribution. Andalso the axial direction pressure distributed equally.Key words Biomass gasification ，Downdraft gasifier, Numerical simulation , Gasification pressure氣化爐實(shí)驗(yàn)成本的提高,和反復(fù)實(shí)驗(yàn)的可行性降低,引言同時(shí)在高溫工況下，人員安全問(wèn)題無(wú)法得到有效的生物質(zhì)氣化"是生物質(zhì)熱化學(xué)轉(zhuǎn)換的關(guān)鍵技保證,因此,對(duì)大型氣化爐模擬研究工作十分必要。術(shù)之一,在氣化爐大型化以后,伴隨而來(lái)的是生物質(zhì)國(guó)內(nèi)外學(xué)者做了大量有關(guān)氣化爐數(shù)值模擬方面中國(guó)煤化工收稿日期: 2009-12-24修回日期: 2010-01 -05*山東省自然科學(xué)基金資助項(xiàng)目(20092RA01100)MHCNMHG作者簡(jiǎn)介:孫宏宇,博士生,主要從事生物質(zhì)能開(kāi)發(fā)及利用研究，E-mail:bbe-119@163.com通訊作者:董玉平,教授,博士生導(dǎo)師,主要從事生物質(zhì)能開(kāi)發(fā)及利用研究，E-mail: dongyp@ sdu. edu. en第11期孫宏宇等:基于Fluent的固定床生物質(zhì)氣化爐冷態(tài)壓力場(chǎng)研究95的研究,國(guó)內(nèi)的研究主要集中于煤氣化工程的實(shí)驗(yàn)動(dòng)量方程在慣性坐標(biāo)系中i方向上的動(dòng)量守恒和模擬分析(2-41) ,對(duì)煤氣化爐溫度、氣化壓力影響機(jī)方程為理、氣化劑滯留時(shí)間對(duì)煤氣化過(guò)程和燃?xì)饨M分的影2(ou,) + -(pu,4)=響以及氣化壓力對(duì)痕量元素的遷移規(guī)律進(jìn)行了分x析。在生物質(zhì)氣化方面,車麗娜等對(duì)上吸式氣化爐p,. +pg: +F:(2)進(jìn)行了建模和模擬,得出爐層高度對(duì)燃?xì)獬煞趾蜖tax;內(nèi)混合溫度的影響規(guī)律[5]。Sadaka等對(duì)雙相流化式中-靜壓應(yīng)力張量床氣化爐進(jìn)行了數(shù)值模擬[°。高楊等使用Aspeng[一i方向上的重力體積力和外部體積Plus平臺(tái)模擬流化床生物質(zhì)氣化制氫過(guò)程”。國(guó)外力,F包含了模型的相關(guān)源項(xiàng)研究下吸式生物質(zhì)氣化爐的文獻(xiàn)較多,Paulof8]等對(duì)由于生物質(zhì)原料孔隙不均勻,且上部有攪拌器以木材為床料的下吸式生物質(zhì)氣化爐的一部分 工作轉(zhuǎn)動(dòng),氣化劑進(jìn)入爐內(nèi)后運(yùn)動(dòng)極不規(guī)則,極不穩(wěn)定,參數(shù)進(jìn)行了模擬分析,得到了生物質(zhì)氣化參數(shù)的變每一點(diǎn)的速度隨機(jī)變化著,因此其流態(tài)應(yīng)選用湍流化對(duì)氣化強(qiáng)度的影響。模型,本文選用標(biāo)準(zhǔn)Realizable k-ε湍流模型模擬從工業(yè)分析和元素分析來(lái)看,生物質(zhì)與煤有相氣相湍流運(yùn)輸[°。當(dāng)大的區(qū)別,在研究中不能完全按照煤氣化方法來(lái)1.2 網(wǎng)格劃分進(jìn)行,氣化爐爐型的不同在氣化過(guò)程中原料燃燒熱因氣化爐整體結(jié)構(gòu)較復(fù)雜,為方便而準(zhǔn)確地進(jìn)解方式和配風(fēng)工藝也不相同,而且國(guó)外大多僅對(duì)以行數(shù)值模擬,對(duì)氣化爐作了簡(jiǎn)化處理,建模時(shí)省去了木材為床料的下吸式生物質(zhì)氣化爐各項(xiàng)工作參數(shù)進(jìn)工藝上的圓角。爐體高度為2.3 m,直徑為1.2 m;行了模擬分析,沒(méi)有涉及到低品質(zhì)秸稈床料氣化爐。填料層高度 1.8m,上、下層配風(fēng)管各為8個(gè),均勻本研究針對(duì)上述問(wèn)題,對(duì)產(chǎn)氣量為780 Nm'/h水 平圓周分布,分別位于距底部2.0m和1.0m處，以稻殼為原料的下吸式固定床秸稈氣化爐內(nèi)部壓力直徑為0.05m;在Gambit建立三維實(shí)體模型,對(duì)爐場(chǎng)和氣流場(chǎng)在不同配風(fēng)工況條件下進(jìn)行數(shù)值模擬分體和配風(fēng)管分別用非結(jié)構(gòu)四面體網(wǎng)格和六面體網(wǎng)格析,再經(jīng)過(guò)多點(diǎn)測(cè)壓實(shí)驗(yàn)驗(yàn)證模擬結(jié)果的可靠性,為劃分,共有707595個(gè)單元網(wǎng)格。生物質(zhì)氣化爐模擬分析提供依據(jù)。1.3數(shù)值解法及 邊界條件對(duì)于氣固兩相流冷態(tài)模擬，研究人員曾提出多.1數(shù)值模擬種方法,應(yīng)用較為廣泛的是混合多相模型和歐拉多1.1數(shù)學(xué)模型相模型,本文采用精度較高的歐拉-拉格朗日法處理氣化爐結(jié)構(gòu)簡(jiǎn)圖如圖1所示。氣化爐反應(yīng)區(qū)域多相流模擬。爐內(nèi)料層可視作各向同性均勻多孔介質(zhì)模型‘0],根據(jù)原料堆積密度與稻r_.空氣殼自身密度關(guān)系得出填料層孔隙率為0.3,再根據(jù)120料位稻殼自身密度計(jì)算得出其當(dāng)量直徑為3.12mm。在多相流模擬中,將料層設(shè)置為稻殼屬性填充。采用多孔介質(zhì)模型來(lái)仿真料層結(jié)構(gòu),多孔介質(zhì)具有粘性阻力和慣性阻力,粘性阻力為滲透率的倒數(shù)_D(3a = 150(1-8)2 .式中a---滲透率D,-- 顆粒當(dāng)量直徑ε一床層空 隙率圖1生物質(zhì)氣化 爐簡(jiǎn)圖慣性阻力的計(jì)算公式可以用滲透率的計(jì)算公式Fig. 1 Diagram of the biomass gasifier來(lái)表達(dá)本文采用基于有限體積法的CFD3.51-ε4)( computational fluid dynamics)商用軟件Fluent進(jìn)行中國(guó)煤化工計(jì)算,氣化爐內(nèi)的氣體流動(dòng)由質(zhì)量、動(dòng)量守恒方程描CNMHG用Fluent軟件對(duì)單述。連續(xù)性方程的一般形式為[”層爐和雙層爐模型進(jìn)行對(duì)比模擬分析。在料層中軸°+&(pu,)=S.(1)線上自底部向上設(shè)置4層12個(gè)壓力監(jiān)測(cè)點(diǎn),由上至下各層壓力監(jiān)測(cè)點(diǎn)基本處于干燥層熱解層、氧化層96農(nóng)業(yè)機(jī)械學(xué)報(bào)2010年及還原層的相應(yīng)位置,其高度如圖1所示,且各點(diǎn)的徑向距離相等。各項(xiàng)收斂參差精度設(shè)置為10~3,達(dá)配風(fēng)管到收斂時(shí)連續(xù)相及速度都達(dá)到了10-*。測(cè)壓點(diǎn)2仿真結(jié) 果與實(shí)驗(yàn)驗(yàn)證_測(cè)壓管模型選取爐側(cè)配風(fēng)管水平對(duì)吹,基于同向均勻多孔介質(zhì)模型的設(shè)定,在結(jié)果云圖中只取爐體正中圖4氣化爐及其測(cè)試點(diǎn)軸切面顯示壓力場(chǎng)和氣流場(chǎng)。圖2為收斂后單層配Fig.4 Gasifier and its test points風(fēng)工況下料層縱向壓力云圖,壓力集中于料層上部1/4區(qū)域;圖3為雙層配風(fēng)工況下料層縱向壓力云下的壓力。實(shí)驗(yàn)與模擬的誤差為圖。從圖2中看到,壓力集中區(qū)域不再明顯,且圖1中所顯示的爐體上方壓力集中區(qū)域的壓力值有所減σ=、會(huì)((*. -*.)?/n(5)馬。式中x,實(shí)驗(yàn)值x___模擬值n- -測(cè)點(diǎn)數(shù)計(jì)算σ時(shí)剔除最大偏差,分別代人各層測(cè)得的壓力數(shù)據(jù),求得相應(yīng)的絕對(duì)誤差和相對(duì)誤差結(jié)果,經(jīng)計(jì)算得:干燥層誤差為0. 12 kPa(0. 52%),熱解層0.15 kPa(0.95%) ,氧化層0.16 kPa(1.18%)，還原層0.18kPa(2.47%)。氧化層、還原層誤差相對(duì)較大,這是因?yàn)樯镔|(zhì)散料在爐內(nèi)分布不均勻,處于氣化爐下方的床層密度較高,不能完全滿足各向同性.均勻多孔介質(zhì)模型。圖2單層配風(fēng)工況 氣化爐床層壓力云圖對(duì)比曲線圖及誤差分析說(shuō)明模擬壓力值與實(shí)際Fig.2 Contours of static pressure in壓力值相差不大。多孔介質(zhì)模型可以對(duì)實(shí)際工況進(jìn)single-layer air duct gasifer行仿真分析。在雙層配風(fēng)工況下,氣化爐內(nèi)部氧化層、還原層和熱解層的壓力高于單層管配風(fēng),而干燥層則相反，圖5所示的軸向壓力值曲線,在距爐排0.3~1 m處雙層配風(fēng)的實(shí)驗(yàn)和模擬曲線均位于單層配風(fēng)上方，其結(jié)果與模擬結(jié)果相一致。一模擬結(jié)果(單)25。-模擬結(jié)果(雙)---實(shí)驗(yàn)結(jié)果(單)ζ20 --鎮(zhèn)( FEX每1圖3雙層配風(fēng)管氣化爐床層壓力云圖E 10Fig. 3 Contours of statie pressure indouble-layer air duct gasifier3 0.6 0.9 12 1.5 1.8應(yīng)用氣化爐多點(diǎn)測(cè)壓實(shí)驗(yàn)驗(yàn)證模擬的準(zhǔn)確性位置/m時(shí),根據(jù)模型的監(jiān)測(cè)點(diǎn)位置,應(yīng)用美國(guó)基康公司生產(chǎn)圖5各層壓力實(shí)驗(yàn)值與模擬值比較曲線的4500MLP型測(cè)壓管,在氣化爐中對(duì)12個(gè)監(jiān)測(cè)點(diǎn)Fig.5 Comparison of the experimental壓力進(jìn)行冷態(tài)檢測(cè),實(shí)驗(yàn)時(shí),壓力管進(jìn)人以稻殼為原and simulation data料的氣化爐內(nèi)部0.6 m,待壓力穩(wěn)定以后記下數(shù)據(jù)生物質(zhì)氣化討程中釘化層和還原層是產(chǎn)生燃并與模擬值進(jìn)行比較,測(cè)壓位置與圖1中模擬分析氣的中國(guó)煤化工為，氣化過(guò)程是一一個(gè)中的測(cè)壓點(diǎn)相對(duì)應(yīng)。氣化爐測(cè)壓實(shí)驗(yàn)位置如圖4所復(fù)雜:fYHCNMHG式為示。w=kAAp"-I(6)氣化爐4排測(cè)壓點(diǎn)位于實(shí)際運(yùn)行爐內(nèi)的4個(gè)反(RT)應(yīng)層,實(shí)驗(yàn)值和模擬值描述了各層在不同配風(fēng)條件式中w一反應(yīng)速率R-一氣體常數(shù)第11期孫宏宇等:基于Fluent的固定床生物質(zhì)氣化爐冷態(tài)壓力場(chǎng)研究97A,一-氧氣的相對(duì)濃度雙層爐內(nèi)氣流場(chǎng)如圖7所示。由于一部分氣化A2--原料的相對(duì)濃度劑由.上層管供給,下層配風(fēng)管進(jìn)氣量減少,料層內(nèi)氣T反應(yīng)物的溫度化劑流速趨向平均。以此推斷,壓力場(chǎng)模擬結(jié)果中在反應(yīng)物濃度和反應(yīng)溫度-定時(shí),氣化反應(yīng)速雙層配風(fēng)管氣化爐內(nèi)氣化層下方壓力增大的因素主率與反應(yīng)區(qū)域壓力的n-1次方呈正比。氧化層的要是上下配風(fēng)管分流人風(fēng),降低了熱分解層以下部壓力提高有利于氧化反應(yīng)速率的加快,在氣化劑停分空氣流速。使得壓力值提高。留時(shí)間不變的情況下,反應(yīng)過(guò)程更加完全,提高了氧化區(qū)的溫度;使還原區(qū)溫度升高,并且在壓力增加的條件下,還原區(qū)反應(yīng)速率加快,基于以上兩點(diǎn),根據(jù).文獻(xiàn)[11]所述，壓力值增加,生物質(zhì)燃?xì)庵锌扇冀M分將有所提高,并且有利于降低出爐燃?xì)獾慕褂秃?結(jié)果分析通過(guò)流速場(chǎng)分析,可研究單、雙層配風(fēng)工況氣化爐內(nèi)壓力場(chǎng)產(chǎn)生變化的原因。圖7雙層配風(fēng)管氣化爐料層內(nèi)部流場(chǎng)云圖Fig.7 Contours of velocity in double-layer air duct gasifier根據(jù)伯努利方程["2],流速與壓力呈反比。由圖6單層爐內(nèi)氣流場(chǎng)可以看出,配風(fēng)口進(jìn)風(fēng)速度高，且氣化爐出口壓力為負(fù)壓,因此,氣化劑風(fēng)速場(chǎng)集中4結(jié)論于下方的熱分解層和氧化還原層,干燥層區(qū)域氣流(1)模擬和實(shí)驗(yàn)結(jié)果較為一致,最大相對(duì)誤差速度較低。在2.5%以下,表明歐拉多相流模型以及多孔介質(zhì).模型相結(jié)合的方法可以計(jì)算生物質(zhì)氣化爐內(nèi)部壓力場(chǎng)。(2)雙層配風(fēng)狀態(tài)下,氧化層和還原層中壓力比單層配風(fēng)狀態(tài)提高了5 ~ 10 kPa。(3)根據(jù)反應(yīng)動(dòng)力學(xué)理論和溫度對(duì)氣化反應(yīng)影響機(jī)理,間接得出氧化區(qū)和還原區(qū)壓力的提高對(duì)優(yōu)化燃?xì)饨M分的作用。(4)基于冷靜態(tài)工況進(jìn)行了模擬研究,對(duì)于實(shí)圖6單層配風(fēng)管氣化爐料層 內(nèi)部流場(chǎng)云圖際運(yùn)行過(guò)程中的熱態(tài)情況,可利用本研究的模擬方Fig.6 Contours of velocity in single-layer法,通過(guò)改變孔隙率及相關(guān)溫度參數(shù)進(jìn)行模擬,因此air duet gasifier為熱態(tài)模擬過(guò)程計(jì)算模型的選擇提供了依據(jù)。參考文獻(xiàn)1吳創(chuàng)之,周肇秋,陰秀麗,等.我國(guó)生物質(zhì)能源發(fā)展現(xiàn)狀與思考[J].農(nóng)業(yè)機(jī)械學(xué)報(bào),2009 ,40(1):91 -99.Wu Chuangzhi, Zhou Zhaoqiu, Yin Xiuli, et al. Current status of biomass energy development in China[ J]. Transactions ofthe Chinese Society for Agricultural Machinery, 2009，40(1):91 ~ 99. (in Chinese)黃亞繼.金保升,仲兆平,等.氣化壓力對(duì)煤氣化過(guò)程中痕量元表遷移規(guī)律的影響[J].東南大學(xué)學(xué)報(bào):自然科學(xué)版, .2008 ,38(1):92 ~96.Huang Yaji, Jin Baosheng, Zhong Zhaoping， et al. Efect of gasification pressure on the ocurrence of trace elements[J].Journal of Southeast University: Natural Science Edition, 2008 ,38(1): 92 ~96. (in Chinese)吳學(xué)成,王勤輝,駱仲?zèng)Q,等.氣化參數(shù)影響氣流床煤氣化的模型研空(1)-越刑建立乃驗(yàn)證[J].浙江大學(xué)學(xué)報(bào):工學(xué)版,2004 ,38(10):1 483 ~ 1489.中國(guó)煤化工Wu Xuecheng，Wang Qinhui, Luo Zhongyang, et al. ModelingHCN M H G on entrained flow coalgasification ( I ): model prediction and analysis[J]. Journal of Zhejiang University: Engineering Science, 2004,38( 10):1 483~ 1 489. (in Chinese)(下轉(zhuǎn)第104頁(yè))104農(nóng)業(yè)機(jī)械學(xué)報(bào)2010年14張全國(guó), 雷廷宙.農(nóng)業(yè)廢棄物氣化技術(shù)[M].北京:化學(xué)工業(yè)出版社,2006 :209 ~211.15 Carlsen H, Ammundsen N, Traerup J. 40 kW stirling engine for solid fuel[ C] // Energy Conversion Engineering Conference,1996. Proceedings of the 3Ist Intersociety, IEEE: 1996,2:1 301 ~ 1 306.16 Gaun A，Schmautzer E. Biomss-fuelled stirling micro combined heat and power plants[ C] // ICCEP'07 InternationalConference on Clean Electrical Power, IEEE, 2007 :429 -432.17 翁一武,蘇明,翁史烈.先進(jìn)微型燃?xì)廨啓C(jī)的特點(diǎn)與應(yīng)用前景[J].熱能動(dòng)力工程,2003,18(2):111 -116.Weng Yiwu, Su Ming, Weng Shilie. Specifie features of advanced micro gas turbines and their application prospects[J].Journal of Engineering for Thermal Energy and Power, 2003, 18(2):111 -116. ( in Chinese)18 Francisco J, Antonio C, Jose C. Biomass based micro-turbine plant and distribution network stability[J]. Energy Conversionand Management, 2004, 45(17):2713 ~2727.19 Cano A, Jurado F, Carpio J. Modelling of power plants based on gasifier/ gas turbine technologies[ C]. 2002 IEEEAfricon-6th Africon Conference in Africa, 2002 ,2 :797 ~ 802.20 黃艷琴,陰秀麗,吳創(chuàng)之.生物質(zhì)氣化高溫燃料電池-體化發(fā)電技術(shù)[J].可再生能源,2006(6) :43 -47.Huang Yanqin, Yin Xiuli, Wu Chuangzhi. Status of integrated biomass gasification and fuel cell power generation system[J]. Renewable Energy Resources, 2006(6):43 ~47 . (in Chinese)21 Gomez M, Jurado F. Feasibility of fuel ell systems using forest residues[ R ] // Power Engineering Society General Meeting,2007. IEEE, 2007:1 ~7.22 Kirubakaran A, Shailendra Jain, Nema R K. A review on fuel cell technologies and power electronic interface [J]. .Renewable and Sustainable Energy Reviews ,2009 ,13(9):2 430 ~ 2440.23 中國(guó)能源年鑒編輯委員會(huì)，中國(guó)能源年鑒2005/2006[M]. 北京:科學(xué)出版社,2007 :256.24 吳創(chuàng)之,周肇秋,陰秀麗,等. 我國(guó)生物質(zhì)能源發(fā)展現(xiàn)狀與思考[J]. 農(nóng)業(yè)機(jī)械學(xué)報(bào),2009 ,40(1):91 -99.Wu Chuangzhi, Zhou Zhaoqiu，Yin Xiuli, et al. Current status of biomass energy development in China[J]. Transations ofthe Chinese Society for Agricultural Machinery, 2009 ,40(1):91 ~ 99. (in Chinese). (上接第97頁(yè))4 Liu Guisu, Tate A C, Bryant c w, et al. Mathematical modeling of coal char reactivity with CO2 at high pressures andtemperatures[J]. Fuel ,2000 ,79(10):1 145~1 154.5車麗娜,王維新.上吸式生物質(zhì)氣化爐的建模和模擬[J].農(nóng)機(jī)化研究,2008(8):55~57.6 SadakaS S, Ghaly A E, Sabbah M A. Two phase biomass air-steam gasification model for fuidized bed reactors: part 1-model development[J]. Biomass and Bioenergy, 2002, 22(6): 436 ~ 441.7高楊,肖軍,沈來(lái)宏.串行流化床生物質(zhì)氣化制取富氫氣體模擬研究[J]. 太陽(yáng)能學(xué)報(bào),2008 ,29(7) :894 ~ 899.Gao Yang, Xiao Jun, Shen Laihong. Hydrogen production from biomass gasification in interconected fluidized beds[J]. ActaEnergiae Solaris Sinica, 2008 ,29(7) :894 ~ 899. ( in Chinese)3 Carlos R Altafini, Paulo R W ander, Ronaldo M Barreto. Prediction of the working parameters of a wood waste gasifier throughan equilibrium model[J]. Energy Conversion and Management, 2003, 44(17): 2763 ~2 777.) Franco C, Pinto F, Gulyurtlu 1, et al. The study of reactions infuencing the biomass steam gasification process[J]. Fuel,2003 ,82(7) :835 ~ 842.10肖軍,沈來(lái)宏,鄭敏,等.基于TG-FTIR的生物質(zhì)加壓熱解實(shí)驗(yàn)研究[J].太陽(yáng)能學(xué)報(bào),2007,28(9):972~978.Xiao Jun, Shen Laihong, Zheng Min, et al. TG - FTIR analysis of pressurized pyrolysis of biomass[J]. Acta EnergiaeSolaris Sinica, 2007 ,28(9) :972 ~978. ( in Chinese)Mathieu P, Dubuisson R. Performance analysis of a biomass gasifier[J]. Energy Conversion and Management, 2002 ，43(9-12):1 291 ~1 294. .12管國(guó)錚,趙汝溥.化工原理[M].北京:化學(xué)工業(yè)出版社,2003.中國(guó)煤化工MYHCNMHG