图1 超临界水气化与传统热解气化的反应势能及反应进程对比[31]

Fig.1 Comparison of reaction potential energy and reaction process between supercritical water gasification and conventional pyrolysis gasification[31]

图2 碱催化与非催化条件下水煤气变换反应在Arrhenius方程中拟合速率常数的比较[50]

Fig.2 Comparison of fitted rate constants in the Arrhenius equation for water-gas conversion reactions under alkali-catalyzed and non-catalyzed conditions[50]

图3 稀释黑液在不同连续式反应器的超临界水气化效果(a) 23 MPa,600~700℃,0.81%(质量)[61]; (b) 25 MPa,400~600℃,2.5%(质量)[38]

Fig.3 Supercritical water gasification of dilute black liquor in different continuous reactors(a) 23 MPa, 600—700℃, 0.81%(mass)[61]; (b) 25 MPa, 400—600℃, 2.5%(mass) [38]

图4 稀释黑液超临界水气化反应后的颜色[38](25 MPa,400~600℃,2.5%(质量))

Fig.4 Color of dilute black liquor after supercritical water gasification reaction [38](25 MPa, 400—600℃, 2.5%(mass))

图5 不同温度下的间歇釜式反应器超临界水气化[62](25 MPa,600~750℃,9.5%(质量))

Fig.5 Supercritical water gasification in an intermittent batch reactor at different temperatures[62](25 MPa, 600—750℃, 9.5%(mass))

图6 不同温度和压力条件下石英管反应器里的碳气化率[60](22~40 MPa,375~650℃,2.5%(质量))

Fig.6 Carbon gasification efficiency in the quartz tube reactor at different temperature and pressure conditions [60](22—40 MPa, 375—650℃, 2.5%(mass))

图7 连续式反应器不同进料浓度下的氢气产量(a)和COD去除率(b) [61](23 MPa,600~700℃,0.81%~2.43%(质量))(23 MPa, 600—700℃, 0.81%—2.43%(mass))

Fig.7 Hydrogen yield (a) and COD removal ratio (b) for a continuous reactor with different feed concentrations [61]

图8 间歇式反应器里不同浓度条件下气体组成和碳气化率[62](23~26 MPa,750℃,2.5%~9.5%(质量))

Fig.8 Gas composition and carbon gasification efficiency at different concentration conditions in the intermittent reactor[62](23—26 MPa, 750℃, 2.5%—9.5%(mass))

图9 不同停留时间的气体组分比例和碳气化率[62](23~26 MPa,700℃,9.5%(质量))

Fig.9 Gas fraction and carbon gasification efficiency for different residence times[62](23—26 MPa, 700℃, 9.5%(mass))

图10 连续式反应器里不同停留时间的气体组分占比(a)和COD去除率(b) [38](25 MPa,600℃,9.5%(质量))(25 MPa, 600℃, 9.5%(mass))

Fig.10 Gas fraction (a) and COD removal ratio (b) for different residence time in the continuous reactor [38]

图11 不同金属氧化物对造纸黑液超临界水气化碳气化率的影响[39](600℃,12.6%(质量),24~26 MPa)(600℃, 12.6%(mass), 24—26 MPa)

Fig.11 Effect of different metal oxides on the carbon gasification efficiency of black liquor supercritical water gasification[39]

图12 不同金属氧化物对黑液超临界水气化氢气产量的影响[39](600℃,12.6%(质量),24~26 MPa)

Fig.12 Effect of different metal oxides on the hydrogen yield of black liquor supercritical water gasification [39] (600℃, 12.6%(mass), 24—26 MPa)

图13 气相条件下的硫酸盐还原反应体系及能垒[76]

Fig.13 Sulfate reduction reaction scheme and energy barrier under gas phase conditions[76]

图14 超临界水条件下硫酸盐还原反应体系及能垒[76]

Fig.14 Sulfate reduction reaction scheme and energy barrier under supercritical water conditions[76]

图15 两类盐水系统相图:（a）1类盐水系统;（b）2类盐水系统[80]

Fig.15 Phase diagram of two types of brine systems: (a) Type 1 brine system; (b) Type 2 brine system [80]

图16 超临界水无机盐分离器示意图[83-85]

Fig.16 Schematic diagram of supercritical water inorganic salt separator[83-85]

图17 无机盐回收随K/(K+Na)的变化规律[86]

Fig.17 Variation pattern of inorganic salt recovery with K/(K+Na)[86]

图18 西安交通大学动力工程多相流国家重点实验室间歇反应器[14,40]系统示意图1—Ar气瓶;2—压力传感器;3—温度传感器;4—数据采集站;5—湿气流量计;6—间歇釜;7—电炉

Fig.18 Schematic diagram of the intermittent reactor[14,40] system at the State Key Laboratory of Multiphase Flow in Power Engineering, Xi'an Jiaotong University1—Ar gas bottle; 2—pressure sensor; 3—temperature sensor; 4—data acquisition station; 5—wet gas flow meter; 6—intermittent kettle; 7—electric furnace

图19 连续管流式超临界水气化制氢实验装置示意图[38]

Fig.19 Schematic diagram of the experimental setup for continuous tubular flow supercritical water gasification to hydrogen[38]

图20 连续式流态化超临界水气化制氢反应装置示意图

Fig.20 Schematic diagram of continuous fluidized supercritical water gasification reactor for hydrogen