燃煤机组脱硫废水零排放物料-能-水耦合机制及优化

doi:10.11949/0438-1157.20210694

化工学报 ›› 2021, Vol. 72 ›› Issue (11): 5800-5809.DOI: 10.11949/0438-1157.20210694

燃煤机组脱硫废水零排放物料-能-水耦合机制及优化

陈程¹(),陈鑫²,徐凤³,吴斌¹,李元媛²,陆规²()

^1.中国能源建设集团江苏省电力设计院有限公司，江苏南京 211102
^2.华北电力大学能源动力与机械工程学院，北京 102206
^3.中国能源建设集团安徽省电力设计院有限公司，安徽合肥 230022

收稿日期:2021-05-21 修回日期:2021-06-21 出版日期:2021-11-05 发布日期:2021-11-12
通讯作者: 陆规
作者简介:陈程（1987—），女，博士，高级工程师，chencheng@jspdi.com.cn
基金资助:
中国能源建设集团众筹科技(CEEC-ZC-2018-011);国家自然科学基金项目(51876057)

Matter-energy-water coupling mechanism and optimization for zero discharge of desulfurization wastewater from coal-fired units

Cheng CHEN¹(),Xin CHEN²,Feng XU³,Bin WU¹,Yuanyuan LI²,Gui LU²()

^1.China Energy Construction Group Jiangsu Electric Power Design Institute Co. , Ltd. , Nanjing 211102, Jiangsu, China
^2.School of Energy Power and Mechanical Engineering, North China Electric Power University, Beijing 102206, China
^3.China Energy Construction Group Anhui Electric Power Design Institute Co. , Ltd. , Hefei 230022, Anhui, China

Received:2021-05-21 Revised:2021-06-21 Online:2021-11-05 Published:2021-11-12
Contact: Gui LU

摘要/Abstract

摘要：

湿法脱硫排出的废水是燃煤机组废水中最难处理的末端废水之一。热法固化是实现脱硫废水零排放的必然途径。通过构建整个燃煤机组厂级尺度热力系统虚拟仿真模型，从能量流、物料流、水平衡及其之间的相互影响机制的角度对比分析了目前三种主流不同脱硫工艺路线的优劣。在此基础上，提出了基于吸附式热泵和多效蒸馏浓缩，废热用于干燥的新型脱硫工艺，新工艺所需的高温烟气量最小，仅为旁路直喷式的1/5，为目前主流浓缩干燥方案的1/3，在回收水分的同时，极大降低高温烟气的消耗量，降低对主机安全性的影响。相关研究可以为燃煤机组脱硫废水零排放及深度节水提供新的解决思路。

关键词: 脱硫废水, 零排放, 物料-水-能耦合, 多效蒸馏, 吸收式热泵

Abstract:

The waste water discharged from wet desulfurization is one of the most difficult terminal waste water in the waste water of coal-fired units. Thermal curing is the inevitable way to achieve zero discharge of desulfurization wastewater. By constructing a virtual simulation model of the whole coal-fired unit plant-scale thermal system, the advantages and disadvantages of the three mainstream different FGD process routes are compared and analyzed from the perspectives of energy flow, material flow, water balance, and their mutual influence mechanisms. On this basis, a new desulfurization process with heat pump and multi-effects distill is proposed, which requires the smallest amount of high-temperature flue gas, only 1/5 of the bypass direct injection type, and 1/3 of the current mainstream concentration and drying scheme. The new process significantly reduces the consumption of high-temperature flue gas while recovering water and increasing the host's safety. The related research can provide new solution ideas for eliminating desulfurization wastewater from coal-fired units and deep water-saving and provide quantitative analysis and optimization methods.

Key words: desulfurization wastewater, zero discharge, material-water-energy coupling, multi-effect distillation, absorption heat pump

中图分类号:

TK 223.33

陈程, 陈鑫, 徐凤, 吴斌, 李元媛, 陆规. 燃煤机组脱硫废水零排放物料-能-水耦合机制及优化[J]. 化工学报, 2021, 72(11): 5800-5809.

Cheng CHEN, Xin CHEN, Feng XU, Bin WU, Yuanyuan LI, Gui LU. Matter-energy-water coupling mechanism and optimization for zero discharge of desulfurization wastewater from coal-fired units[J]. CIESC Journal, 2021, 72(11): 5800-5809.

图/表 14

图1 燃煤机组厂级尺度热力学耦合模型

Fig.1 Plant-scale thermodynamic coupling model for coal units

表1 600 MW电厂模型验证

Table 1 Validation of 600 MW power plant model

指标	烟气温度/℃						给水温度/℃
指标	前屏出口	后屏出口	高再出口	高过出口	低再出口	省煤器出口	给水温度/℃
设计	1124.91	1020	900	785	515	296.04	280.4
模拟	1244	1137	964	683	512	296	260
误差	9.60%	11.5%	6.64%	13.00%	0.58%	0	7.31%
指标	温升/℃						总功率/ kW
指标	#7、#8	#6	#5	#1	#2	#3	总功率/ kW
设计	47	20	40	20	30	30	600000
模拟	57	20	39	20	30	33	604890
误差	21.30%	0	2.50%	0	0	10%	0.81%

图2 脱硫废水处理技术路线图

Fig.2 Desulfurization Wastewater Treatment Technology Roadmap

表2 干燥塔进出口物料

Table 2 Drying tower inlet and outlet parameters

物质名称	单位	喷入前脱硫废水	喷入后脱硫废水
water	kg·h^-1	15953.9	1.1
SO₂	kg·h^-1	3.32×10^-9	0.0014
$H S O_{3}^{-}$	kg·h^-1	0.037	0.034
$S O_{4}^{2 -}$	kg·h^-1	6288.8	6823.5
$S O_{3}^{2 -}$	kg·h^-1	53.9	58.4
$C O_{3}^{2 -}$	kg·h^-1	1073.5	1218.2
$H C O_{3}^{-}$	kg·h^-1	950.0	919.1
CaSO₄(s)	kg·h^-1	32.0	31.1
Cl^-	kg·h^-1	246.6	267.5
总流量	kg·h^-1	28452.5	13825.4

表2 干燥塔进出口物料

Table 2 Drying tower inlet and outlet parameters

物质名称	单位	喷入前脱硫废水	喷入后脱硫废水
water	kg·h^-1	15953.9	1.1
SO₂	kg·h^-1	3.32×10^-9	0.0014
$H S O_{3}^{-}$	kg·h^-1	0.037	0.034
$S O_{4}^{2 -}$	kg·h^-1	6288.8	6823.5
$S O_{3}^{2 -}$	kg·h^-1	53.9	58.4
$C O_{3}^{2 -}$	kg·h^-1	1073.5	1218.2
$H C O_{3}^{-}$	kg·h^-1	950.0	919.1
CaSO₄(s)	kg·h^-1	32.0	31.1
Cl^-	kg·h^-1	246.6	267.5
总流量	kg·h^-1	28452.5	13825.4

图3 高温烟气分流量对浓缩倍率和发电量的影响

Fig.3 Effect of high temperature flue gas fractional flow rate on concentration multiplier and power production

图4 低温浓缩-高温干燥模型

Fig.4 Low temperature concentration-high temperature drying model

表3 浓缩-干燥法进出口物料变化

Table 3 Concentration - drying method of import and export material changes

物质名称	单位	浓缩塔入口废水含量	浓缩塔出口废水含量	干燥塔出口废水含量
water	kg·h^-1	16946.53	9704.90	1.85
SO₂	kg·h^-1	2.03×10^-7	0.61	0.0015
$H S O_{3}^{-}$	kg·h^-1	10.20	1.11	1.11
$S O_{4}^{2 -}$	kg·h^-1	5626.34	4884.68	4884.68
$S O_{3}^{2 -}$	kg·h^-1	47.37	41.12	41.12
$C O_{3}^{2 -}$	kg·h^-1	647.08	488.31	488.31
$H C O_{3}^{-}$	kg·h^-1	1488.19	1443.85	1443.85
CaSO₄(s)	kg·h^-1	33.62	35.42	35.42
Cl^-	kg·h^-1	220.76	191.84	191.84
总流量	kg·h^-1	28452.5	19770.80	10247.29

表3 浓缩-干燥法进出口物料变化

Table 3 Concentration - drying method of import and export material changes

物质名称	单位	浓缩塔入口废水含量	浓缩塔出口废水含量	干燥塔出口废水含量
water	kg·h^-1	16946.53	9704.90	1.85
SO₂	kg·h^-1	2.03×10^-7	0.61	0.0015
$H S O_{3}^{-}$	kg·h^-1	10.20	1.11	1.11
$S O_{4}^{2 -}$	kg·h^-1	5626.34	4884.68	4884.68
$S O_{3}^{2 -}$	kg·h^-1	47.37	41.12	41.12
$C O_{3}^{2 -}$	kg·h^-1	647.08	488.31	488.31
$H C O_{3}^{-}$	kg·h^-1	1488.19	1443.85	1443.85
CaSO₄(s)	kg·h^-1	33.62	35.42	35.42
Cl^-	kg·h^-1	220.76	191.84	191.84
总流量	kg·h^-1	28452.5	19770.80	10247.29

图5 浓缩倍率对高温烟气分流量、发电功率和发电标准煤耗率的影响

Fig.5 Effect of concentration rates on high temperature flue gas fraction flow rate, power, and coal consumption

图6 用于脱硫废水浓缩的多效蒸馏系统模型

Fig.6 Model of multi-effect distillation system for desulfurization wastewater concentration

表4 多效蒸馏进出口物料变化

Table 4 Multi-effect distillation import and export material changes

物质名称	单位	多效蒸馏入口脱硫废水	多效蒸馏出口脱硫废水
water	kg·h^-1	17196.00	9701.67
SO₂	kg·h^-1	2.92×10^-9	0
$H S O_{3}^{-}$	kg·h^-1	0.031	0.030
$S O_{4}^{2 -}$	kg·h^-1	4585.17	4715.64
$S O_{3}^{2 -}$	kg·h^-1	39.78	40.89
$C O_{3}^{2 -}$	kg·h^-1	1459.35	1529.06
$H C O_{3}^{-}$	kg·h^-1	1441.47	1424.68
CaSO₄(s)	kg·h^-1	18.53	18.73
Cl^-	kg·h^-1	179.75	184.86
总流量	kg·h^-1	28452.5	21197.06

表4 多效蒸馏进出口物料变化

Table 4 Multi-effect distillation import and export material changes

物质名称	单位	多效蒸馏入口脱硫废水	多效蒸馏出口脱硫废水
water	kg·h^-1	17196.00	9701.67
SO₂	kg·h^-1	2.92×10^-9	0
$H S O_{3}^{-}$	kg·h^-1	0.031	0.030
$S O_{4}^{2 -}$	kg·h^-1	4585.17	4715.64
$S O_{3}^{2 -}$	kg·h^-1	39.78	40.89
$C O_{3}^{2 -}$	kg·h^-1	1459.35	1529.06
$H C O_{3}^{-}$	kg·h^-1	1441.47	1424.68
CaSO₄(s)	kg·h^-1	18.53	18.73
Cl^-	kg·h^-1	179.75	184.86
总流量	kg·h^-1	28452.5	21197.06

图7 低温烟气热量对不同浓缩方式的影响

Fig.7 Effect of low temperature flue gas heat on different concentration methods

图8 新型吸收式热泵驱动多效蒸馏浓缩干燥脱硫废水处理工艺

Fig.8 Absorption heat pump driven multi-effect distillation concentration drying desulfurization wastewater treatment process

图9 入口脱硫废水预热温度对系统热消耗的影响

Fig.9 Effect of inlet desulfurization wastewater preheating temperature on system heat consumption

表5 四种工艺路线定量对比

Table 5 Quantitative comparison of four process routes

技术路线	消耗热量/kW	入口废水流量/(kg·h^-1)	结晶固体/(kg·h^-1)	凝结水含量/(kg·h^-1)	高温烟气热量/kW
旁路烟气+干燥	10323.75	28452.5	13825.39	N/A	10323.75
浓缩塔+干燥	12590.74	28452.54	10247.29	N/A	6695.37
MED +干燥	9142.97	28452.54	12455.26	7208.68	6692.97
MED+热泵+干燥	6213.89	28452.54	12710.46	13208.57	2358.65

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燃煤机组脱硫废水零排放物料-能-水耦合机制及优化

Matter-energy-water coupling mechanism and optimization for zero discharge of desulfurization wastewater from coal-fired units

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