超高效螺旋式厌氧反应器三相流动特性的研究
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摘要
水环境污染和能源紧缺是我国面临的两大难题。将厌氧消化技术用于污水处理,可实现污染治理和能源回收的双重功效。研发超高效螺旋式厌氧反应器(Super-high-rate Spiral Anaerobic Bioreactor, SSAB),有助于提升我国厌氧消化技术水平,推动治污工程发展。本论文采用试验模拟和数学模拟相结合的方法,系统研究了SSAB的能量耗散、床层膨胀、污泥运动和污水流态等三相流动特性,以优化该类反应器的设计和操作,加速该类反应器的工程化应用。主要成果如下：
(1)研究揭示了SSAB的能量耗散特性。
①建立了SSAB能量耗散(能耗)模型：分离单元的能耗模型为ΔE3-5=2.79×10-9ul3；反应单元的能耗模型为：ΔEu2-3=1.1216×10-7ul2Vp+0.02798×10-7ul3Vp (固定态),流化床状态ΔEf2-3=0.5096×10-7ulVp(流化态)；布水单元的能耗模型为ΔE1-2=3.06×10-4ul-3。各单元和整体能耗模型的模拟值与实测值吻合较好,可用于指导同类型厌氧反应器能耗状况的优化。
②分析了SSAB能耗特征：反应单元在气液固三相时的能耗大于液固两相时的能耗。在低表观液速下,反应单元的能耗大于布水单元；而在高表观液速下,反应单元的能耗小于布水单元。SSAB处于固定床状态、液固两相流化床状态、气液固三相流化床状态以及颗粒结团状态时的反应单元的能耗最大值分别为1.13×10-4W、4.54×10-4W、12.00×10-4 W和91.75×10-4W,布水单元能耗的最大值为18.81×10-4 W,反应器整体能耗的最大值为110.56×10-4 W,其中反应单元占83.0%,布水单元占17.0%,分离单元可忽略不计。反应器整体能耗对各参数的敏感性大小依次为颗粒污泥密度(ρp)、表观液速(ul)、污泥量(Vp)、表观气速(ug)和颗粒污泥直径(dp)。能耗的最大值可作为反应器功率匹配的参考依据；参数灵敏度可作为反应器操作的参考依据。
(2)研究揭示了SSAB的床层膨胀特性。
①建立了SSAB床层膨胀模型：max=(380-186.74ul-0.98ug0.7)/ul(固定态);E=(0.435ul0.29-0.38)/(1-0.435ul0.29)×100%(流化态)；床层最大污泥量Vpmax=7850εs;起始流化速度umf=ε03dp2(ρp-ρ1)g/150μ(1-ε0)；起始输送速度ust=(1-εs)ut。所建模型模拟值与实测值吻合良好,可用于指导同类型厌氧反应器的设计和操作优化。
②分析了SSAB的床层膨胀特征：固定态时,ul≤0.45 mm·s-1,E为0,Vpmax为4867 mL(床层有效体积为7850 mL),τmax逐渐逼近860 s(HRT最大值为2222 s)；流化态时,0.45 mm·s-16.88 mm·s-1,颗粒污泥洗出床层。床层处于流化态时,床层E与ul和ug呈正相关,Vpmax和τmax与ul和ug呈负相关,且ul越大,E、Vpmax和τmax越趋于一致,其值分别逼近160%、1860 mL和104 s。E和Vpmax对ul和ug的敏感性较为接近,但τmax对ul的敏感性大于ug。
(3)研究揭示了SSAB的污泥运动特性。
①建立了SSAB污泥运动物理和数学模型。污泥运动可理解为浮升尾流携带颗粒污泥向上转运,返混流携带颗粒污泥向下转运所致的床层各区段的污泥浓度变化。床层上部-中部(ΔV3-ΔV2)和中部-下部(ΔV2-ΔV1)的污泥转运效率比(kt,n/kt,n-1)分别为0.8259和0.7511,污泥转运效率(kt,n-1)分别为0.102-0.315 m3/m3和0.085-0.253 m3/m3。
②分析了SSAB污泥运动模型参数的灵敏度。超高效螺旋式厌氧反应器螺旋区浮升尾流的污泥转运效率对工艺和结构参数的灵敏性依次为螺旋升角(a),螺旋区域外管直径(R),污泥的沉降速率(vs)和基质的升流速度(vl),它与这些参数呈正相关。通过减小α和R可以优化反应器构型;通过缩短HRT可以提升容积效能。
(4)研究揭示了SSAB的污水流态特性。
①SSAB的污水流态为：低负荷下的返混程度较小(D/uL<0.2,N→∞),污水流态趋于平推流；中、高负荷下的返混程度介于平推流和全混流之间(0.35 ②SSAB的流态特征为：反应器总死区平均值为27.99%,其中生物死区平均值为6.98%,水力死区平均值为21.01%。水力死区Vh与水力负荷L和产气速率G之间满足关系式Vh=0.7603L+0.1627G—4.0620(相关系数R2=0.968),容积水力负荷对水力死区的影响大于容积产气速率。
③SSAB的适宜流态为：N≤3.01,即其流态的等容多釜串联级数不宜超过3.01。为兼顾反应器传质效果和容积效能,反应器设计或操作中,可通过优化反应器构型或优化操作参数来调控N值。
Water pollution and energy shortage are two major environmental problems in China. Application of the anaerobic digestion to the wastewater treatment not only control the pollution but also recycle the energy. In order to enhance the technology of anaerobic digestion and promote the engineering of wastewater treatment, we developed the super-high-rate spiral anaerobic bioreactor (SSAB). In this paper, we investigated the three-phase flow characteristics of SSAB, such as energy dissipation, bed expansion, dynamic behaviors of sludge and flow patterns of wastewater, for the optimization of design and operation and accelerating the engineering applcaction of SSAB. The main results were as follows:
(1) Revealing the energy dissipation(△E) characteristics in SSAB
①We established the△E models in SSAB. The△E model for separation unit was△E3-5= 2.79×10-9u13. The△E models for reaction unit included two different submodels. One was△E2-3=1.1216×10-7u12Vp+0.02798×10-7u13Vp under unfludization state, and the other was△Ef2-3=0.5096×10-7u1Vp under fluidization state. The△E model for water distribution unit was△E1-2=3.06×10-4u13. The predicted values calculated from the△E models in SSAB agreed well with the experimental values. According to the above models, we could optimize and control the△E of the same type of anaerobic bioreactor
②We analysed the AE characteristics in SSAB. The AE under gas-liquid-solid three-phase fluidization state was more than△E under liquid-solid two-phase fluidization state for reaction unit. The△E for reaction unit was more than△E for water distribution unit at low superficial liquid velocity. However, the△E for reaction unit was less than△E for water distribution unit at high superficial liquid velocity. The maximum△E values for reaction unit under unfludization state, liquid-solid two-phase fluidization and gas-liquid-solid three-phase fluidization and granular sludge agglomerate state were 1.13×10-4W,4.54×10-4W,12.00×l0-4W and 91.75×l0-4 W, respectively. The maximum△E value for water distribution unit was 18.81×10-4 W. The maximum△E value in SSAB was 110.56×10-4 W, in which the△E for reaction unit accounted for 83.0% and△E for water distribution unit accounted for 17.0%. The△E value for reaction unit was so low as to be neglected. From parametric sensitivity analysis,△E for SSAB was significantly influenced by pp, u1, Vp, ug and dp in turn. The maximum△E value of 110.56×10-4 W was the basic parameter for matching power in SSAB and the parametric sensitivity could provide reference to optimize the operation for SSAB.
(2) Presenting the bed expansion characteristics for SSAB
①The bed expansion models in SSAB were established. The maximum bed contact time between sludge and liquid model (τmax) under unfludization state wasτmax=(380-186.74u1-098ug0.7)/u1. The bed expansion ratio (E) under fludization state was E= (0.435u10.29-0.38)/(1-0.435u10.29)×100%. The maximum bed sludge content (Vpmax) was Vpmax=7850εs. The minimum fluidization velocity (umf) was umf=ε03dp2 (ρp-ρ1)g/150μ(1-ε0). The minimum transportation velocity (umt) was ust=(1-εs)ut. The predicted values calculated from the△E models in SSAB agreed well with the experimental values. Hence, we could use the aboved models to design and optimize the same type of anaerobic bioreactor.
②We investigated the bed expansion characteristics in SSAB. Under nonfluidization state, u was less than 0.45 mm·s-1; E was 0; Vpmax was 4,867 mL, andτmax approached 860 s [with hydraulic retention time (HRT),2,222]. Under fluidization state, u ranged from 0.45 mm·s-1 to 6.88 mm·s-1, and E Vpmax andτmax were 5.28%-255.69%,1368-4559 mL and 104-732 s (with HRT between 145 s and 2,222 s), respectively. Under transportation state, u was larger than 6.88 mm·s-1 and then washout of granular sludge occurred. Under bed fluidization state, E correlated positively with ug and u1, while Vpmax andτmax correlated negatively with ug and u1, and the values for E, Vpmax and Tmax approached 160%,1,860 mL and 104 s, respectively. For E and Vpmax, the sensitivities of ug and u1were close to each other. But forτmax, the sensitivity of u1was more than that of ug.
(3) Researching the dynamic behaviors characteristics of sludge in SSAB
①We established the physical and mathematical models of sludge dynamic behavior in SSAB. The sludge dynamic behavior could be described as follows:upward transport of sludge resulted from the upgoing wake stream, and downward transport of sludge was caused by the back-mixing stream, which led to the sludge concentration changing along bed height. The ratio of sludge transport efficiency for downflow liquid and upfloat biogas(Kt,n/Kt,n-1) between the upper part and the middle part (△V3-△V2) and the middle part and the lower part (△V2-△V1) in reactor bed were 0.8259 and 0.7511, respectively. The sludge transport efficiencies of upfloat biogas (Kt,n-1) of△V3-△V2 and△V2-△V1, were 0.102-0.315m3/m3 (granular sludge/biogas) and 0.0856-0.2532 m3/m3, respectively.
②We analyzed the parametric sensitivity of sludge dynamic behaviors for SSAB. Judged from parametric sensitivity, Kt,n-1 was significantly influenced by spiral angle (a), outer diameters of the spiral zone (R), superficial settling velocity of the sludge (vs) and superficial linear fluid velocity upwards of influent (v1), which correlated positively with vs and v1. Based on the parametric sensitivity analyses, reducing the a and R can optimize the configuration of bioreactor, and shortening the HRT can improve the volume removal efficiency of the bioreactor.
(4) Studying the flow patterns characteristics in SSAB.
①We studied the flow patterns in SSAB. The back-mixing in SSAB was relatively weak at low loading rate and the flow pattern approached to plug flow (D/uL≤0.2, N→∞). The back-mixing at medium and high loading rate were between plug flow and completely mixed flow (0.35≤D/uL≤0.467, 1.82≤N≤2.71). The back-mixing was relatively strong at super-high loading rate and the flow pattern tended to be completely mixed flow (D/uL≥0.2, N→1).
②We studied the flow patterns characteristics in SSAB. The mean value of total dead spaces (Vd,%) in SSAB was 27.99%, in which the dead spaces caused by biomass and hydraulic behaviors accounted for 6.98%and 21.01%, respectively. The relationship among Vh, volumetric hydraulic loading rate(L) and volumetric biogas production rate(G)was:Vh=0.7603L+0.1627G-4.0620 (correlation coefficient R2=0.968), and Vh was greatly influenced by G than by L.
③We studied the optimum flow patterns in SSAB. When N≤3.01, SSAB had the optimum flow patterns. Considering both mass transfer and volume efficiency,N can be adjusted by optimizing the configuration and operation parameters of bioreactor in design and operation of bioreactor.
(1)研究揭示了SSAB的能量耗散特性。
①建立了SSAB能量耗散(能耗)模型：分离单元的能耗模型为ΔE3-5=2.79×10-9ul3；反应单元的能耗模型为：ΔEu2-3=1.1216×10-7ul2Vp+0.02798×10-7ul3Vp (固定态),流化床状态ΔEf2-3=0.5096×10-7ulVp(流化态)；布水单元的能耗模型为ΔE1-2=3.06×10-4ul-3。各单元和整体能耗模型的模拟值与实测值吻合较好,可用于指导同类型厌氧反应器能耗状况的优化。
②分析了SSAB能耗特征：反应单元在气液固三相时的能耗大于液固两相时的能耗。在低表观液速下,反应单元的能耗大于布水单元；而在高表观液速下,反应单元的能耗小于布水单元。SSAB处于固定床状态、液固两相流化床状态、气液固三相流化床状态以及颗粒结团状态时的反应单元的能耗最大值分别为1.13×10-4W、4.54×10-4W、12.00×10-4 W和91.75×10-4W,布水单元能耗的最大值为18.81×10-4 W,反应器整体能耗的最大值为110.56×10-4 W,其中反应单元占83.0%,布水单元占17.0%,分离单元可忽略不计。反应器整体能耗对各参数的敏感性大小依次为颗粒污泥密度(ρp)、表观液速(ul)、污泥量(Vp)、表观气速(ug)和颗粒污泥直径(dp)。能耗的最大值可作为反应器功率匹配的参考依据；参数灵敏度可作为反应器操作的参考依据。
(2)研究揭示了SSAB的床层膨胀特性。
①建立了SSAB床层膨胀模型：max=(380-186.74ul-0.98ug0.7)/ul(固定态);E=(0.435ul0.29-0.38)/(1-0.435ul0.29)×100%(流化态)；床层最大污泥量Vpmax=7850εs;起始流化速度umf=ε03dp2(ρp-ρ1)g/150μ(1-ε0)；起始输送速度ust=(1-εs)ut。所建模型模拟值与实测值吻合良好,可用于指导同类型厌氧反应器的设计和操作优化。
②分析了SSAB的床层膨胀特征：固定态时,ul≤0.45 mm·s-1,E为0,Vpmax为4867 mL(床层有效体积为7850 mL),τmax逐渐逼近860 s(HRT最大值为2222 s)；流化态时,0.45 mm·s-1
(3)研究揭示了SSAB的污泥运动特性。
①建立了SSAB污泥运动物理和数学模型。污泥运动可理解为浮升尾流携带颗粒污泥向上转运,返混流携带颗粒污泥向下转运所致的床层各区段的污泥浓度变化。床层上部-中部(ΔV3-ΔV2)和中部-下部(ΔV2-ΔV1)的污泥转运效率比(kt,n/kt,n-1)分别为0.8259和0.7511,污泥转运效率(kt,n-1)分别为0.102-0.315 m3/m3和0.085-0.253 m3/m3。
②分析了SSAB污泥运动模型参数的灵敏度。超高效螺旋式厌氧反应器螺旋区浮升尾流的污泥转运效率对工艺和结构参数的灵敏性依次为螺旋升角(a),螺旋区域外管直径(R),污泥的沉降速率(vs)和基质的升流速度(vl),它与这些参数呈正相关。通过减小α和R可以优化反应器构型;通过缩短HRT可以提升容积效能。
(4)研究揭示了SSAB的污水流态特性。
①SSAB的污水流态为：低负荷下的返混程度较小(D/uL<0.2,N→∞),污水流态趋于平推流；中、高负荷下的返混程度介于平推流和全混流之间(0.35
③SSAB的适宜流态为：N≤3.01,即其流态的等容多釜串联级数不宜超过3.01。为兼顾反应器传质效果和容积效能,反应器设计或操作中,可通过优化反应器构型或优化操作参数来调控N值。
Water pollution and energy shortage are two major environmental problems in China. Application of the anaerobic digestion to the wastewater treatment not only control the pollution but also recycle the energy. In order to enhance the technology of anaerobic digestion and promote the engineering of wastewater treatment, we developed the super-high-rate spiral anaerobic bioreactor (SSAB). In this paper, we investigated the three-phase flow characteristics of SSAB, such as energy dissipation, bed expansion, dynamic behaviors of sludge and flow patterns of wastewater, for the optimization of design and operation and accelerating the engineering applcaction of SSAB. The main results were as follows:
(1) Revealing the energy dissipation(△E) characteristics in SSAB
①We established the△E models in SSAB. The△E model for separation unit was△E3-5= 2.79×10-9u13. The△E models for reaction unit included two different submodels. One was△E2-3=1.1216×10-7u12Vp+0.02798×10-7u13Vp under unfludization state, and the other was△Ef2-3=0.5096×10-7u1Vp under fluidization state. The△E model for water distribution unit was△E1-2=3.06×10-4u13. The predicted values calculated from the△E models in SSAB agreed well with the experimental values. According to the above models, we could optimize and control the△E of the same type of anaerobic bioreactor
②We analysed the AE characteristics in SSAB. The AE under gas-liquid-solid three-phase fluidization state was more than△E under liquid-solid two-phase fluidization state for reaction unit. The△E for reaction unit was more than△E for water distribution unit at low superficial liquid velocity. However, the△E for reaction unit was less than△E for water distribution unit at high superficial liquid velocity. The maximum△E values for reaction unit under unfludization state, liquid-solid two-phase fluidization and gas-liquid-solid three-phase fluidization and granular sludge agglomerate state were 1.13×10-4W,4.54×10-4W,12.00×l0-4W and 91.75×l0-4 W, respectively. The maximum△E value for water distribution unit was 18.81×10-4 W. The maximum△E value in SSAB was 110.56×10-4 W, in which the△E for reaction unit accounted for 83.0% and△E for water distribution unit accounted for 17.0%. The△E value for reaction unit was so low as to be neglected. From parametric sensitivity analysis,△E for SSAB was significantly influenced by pp, u1, Vp, ug and dp in turn. The maximum△E value of 110.56×10-4 W was the basic parameter for matching power in SSAB and the parametric sensitivity could provide reference to optimize the operation for SSAB.
(2) Presenting the bed expansion characteristics for SSAB
①The bed expansion models in SSAB were established. The maximum bed contact time between sludge and liquid model (τmax) under unfludization state wasτmax=(380-186.74u1-098ug0.7)/u1. The bed expansion ratio (E) under fludization state was E= (0.435u10.29-0.38)/(1-0.435u10.29)×100%. The maximum bed sludge content (Vpmax) was Vpmax=7850εs. The minimum fluidization velocity (umf) was umf=ε03dp2 (ρp-ρ1)g/150μ(1-ε0). The minimum transportation velocity (umt) was ust=(1-εs)ut. The predicted values calculated from the△E models in SSAB agreed well with the experimental values. Hence, we could use the aboved models to design and optimize the same type of anaerobic bioreactor.
②We investigated the bed expansion characteristics in SSAB. Under nonfluidization state, u was less than 0.45 mm·s-1; E was 0; Vpmax was 4,867 mL, andτmax approached 860 s [with hydraulic retention time (HRT),2,222]. Under fluidization state, u ranged from 0.45 mm·s-1 to 6.88 mm·s-1, and E Vpmax andτmax were 5.28%-255.69%,1368-4559 mL and 104-732 s (with HRT between 145 s and 2,222 s), respectively. Under transportation state, u was larger than 6.88 mm·s-1 and then washout of granular sludge occurred. Under bed fluidization state, E correlated positively with ug and u1, while Vpmax andτmax correlated negatively with ug and u1, and the values for E, Vpmax and Tmax approached 160%,1,860 mL and 104 s, respectively. For E and Vpmax, the sensitivities of ug and u1were close to each other. But forτmax, the sensitivity of u1was more than that of ug.
(3) Researching the dynamic behaviors characteristics of sludge in SSAB
①We established the physical and mathematical models of sludge dynamic behavior in SSAB. The sludge dynamic behavior could be described as follows:upward transport of sludge resulted from the upgoing wake stream, and downward transport of sludge was caused by the back-mixing stream, which led to the sludge concentration changing along bed height. The ratio of sludge transport efficiency for downflow liquid and upfloat biogas(Kt,n/Kt,n-1) between the upper part and the middle part (△V3-△V2) and the middle part and the lower part (△V2-△V1) in reactor bed were 0.8259 and 0.7511, respectively. The sludge transport efficiencies of upfloat biogas (Kt,n-1) of△V3-△V2 and△V2-△V1, were 0.102-0.315m3/m3 (granular sludge/biogas) and 0.0856-0.2532 m3/m3, respectively.
②We analyzed the parametric sensitivity of sludge dynamic behaviors for SSAB. Judged from parametric sensitivity, Kt,n-1 was significantly influenced by spiral angle (a), outer diameters of the spiral zone (R), superficial settling velocity of the sludge (vs) and superficial linear fluid velocity upwards of influent (v1), which correlated positively with vs and v1. Based on the parametric sensitivity analyses, reducing the a and R can optimize the configuration of bioreactor, and shortening the HRT can improve the volume removal efficiency of the bioreactor.
(4) Studying the flow patterns characteristics in SSAB.
①We studied the flow patterns in SSAB. The back-mixing in SSAB was relatively weak at low loading rate and the flow pattern approached to plug flow (D/uL≤0.2, N→∞). The back-mixing at medium and high loading rate were between plug flow and completely mixed flow (0.35≤D/uL≤0.467, 1.82≤N≤2.71). The back-mixing was relatively strong at super-high loading rate and the flow pattern tended to be completely mixed flow (D/uL≥0.2, N→1).
②We studied the flow patterns characteristics in SSAB. The mean value of total dead spaces (Vd,%) in SSAB was 27.99%, in which the dead spaces caused by biomass and hydraulic behaviors accounted for 6.98%and 21.01%, respectively. The relationship among Vh, volumetric hydraulic loading rate(L) and volumetric biogas production rate(G)was:Vh=0.7603L+0.1627G-4.0620 (correlation coefficient R2=0.968), and Vh was greatly influenced by G than by L.
③We studied the optimum flow patterns in SSAB. When N≤3.01, SSAB had the optimum flow patterns. Considering both mass transfer and volume efficiency,N can be adjusted by optimizing the configuration and operation parameters of bioreactor in design and operation of bioreactor.
引文
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Monteith H D and Stephenson J P. Mixing efficiencies in full-scale anaerobic digesters by tracer methods[J]. Journal-Water Pollution Control Federation,1981,53:78-84.
Mulcahy L T, Shieh W K Fluidization and reactor biomass characteristics of the denitrification fluidized bed biofilm reactor[J]. Water Research,1987, 21:451-458.
Narayanan C M, Narayan V. Multiparameter models for performance analysis of UASB reactors[J]. Chemical Technolology and Biotechnology,2008, 83(8):1170-1176.
Nardi I R. M Zaiat, Foresti E. Influence of the tracer characteristics on hydrodynamic models of packed-bed bioreactors[J]. Bioprocess Engineering,1999,21:469-476.
Ngian K F, Martin W B. Bed expansion characteristics of liquid fluidized particles with attached microbial growth[J]. Biotechnology and Bioengineering,1980,22:1843-1856.
Oh D I, Song J, Hwang S J, et al. Effects of adsorptive properties of biofilter packing materials on toluene removal[J]. Journal of Hazardous Materials 2009,170(1):144-150.
Olivet D, Valls J, Gordillo M A, et al. Application of residence time distribution technique to the study of the hydrodynamic behaviour of a full-scalewastewater treatment plan plug-flow bioreactor[J]. Journal Chemical Technology and Biotechnology,2005.80:425-432.
Pereboom J H F, Vereijken T L F M. Methanogenic granule development in full scale internal circulation reactors[J]. Water Science and Technology, 1994.30(8):9-21.
Perez M, Romero L L, Nebot E, et al. Colonisation of a porous sintered-glass support in anaerobic thermophilic bioreactors[J]. Bioresource Technology.1997.59:177-183.
Pierre B. Christian F, Rene M. Mixing and phase hold-ups variations due to gas production in anaerobic fluidized-bed digesters:influence on reactor performance[J]. Biotechnology and Bioengineering,1998,60(1):36-43.
Pierre B, Christian F, Rene M. Liquid mixing and phase hold-ups in gas producing fluidized bed bioreactors[J]. Chemical Engineering Science, 1998.53(4):617-627.
Rebac S. van Lier JB. Lens P. et al. Psych rophilic anaerobic treatment of low strength wastewaters [J]. Water Science and Technology,1999.39(5): 203-210.
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