煤地下气化低效的化学反应工程根源：滞留层及通道中的传质与反应

doi:10.11949/0438-1157.20220760

摘要/Abstract

摘要：

煤地下气化技术历经国内外一百多年的实验室研究和大量现场试验仍然存在产率低等关键问题。虽然一些文献认为该技术是未来煤炭利用技术的发展方向，但其至今仍未实现工业应用的现象说明其本身存在尚未被充分关注的关键科学（卡脖子）问题。本文从化学反应工程基本原理出发分析该技术涉及的关键传质与反应过程，并与现代大型地上煤气化技术对比，探讨其工业应用技术挑战的科学根源。

关键词: 煤, 地下气化, 传质, 合成气, 一氧化碳, 二氧化碳

Abstract:

After over 100 years worldwide extensive research and numerous field tests underground coal gasification (UCG) has not been applied in industry even though it had long been asserted to be the future syngas (CO + H₂) production technology with many advantages. Although some literatures believe that this technology is the development direction of future coal utilization technology, the phenomenon that it has not yet achieved industrial application shows that it has a key scientific (neck) problem that has not been fully paid attention to. This work compares the productivity and syngas composition of underground coal gasification field tests with those commonly reported for the main types of industrial gasifies used today and analyzes the drawbacks in the UCG from the principle of mass transfer and reaction in the stagnant boundary layer on the coal surface and in the gasification tunnel.

Key words: coal, underground gasification, mass transfer, syngas, carbon monoxide, carbon dioxide

中图分类号:

TQ 54

刘振宇. 煤地下气化低效的化学反应工程根源：滞留层及通道中的传质与反应[J]. 化工学报, 2022, 73(8): 3299-3306.

Zhenyu LIU. Origin of low productivity of underground coal gasification: diffusion and reaction in stagnant boundary layer and gasification tunnel[J]. CIESC Journal, 2022, 73(8): 3299-3306.

图/表 8

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试验年份和地点	气化通道尺寸			粗煤气产出			有效气产量/ (m³/h)	产气组成/%（有些总和不是100%）
试验年份和地点	长度/ m	断面/ m²	气化面/ m²	产量/ (m³/h)	速率/ (m/h)	热值/ (MJ/m³)	有效气产量/ (m³/h)	CO	H₂	CO₂	CH₄	O₂	N₂
1948美国高尔加斯	90	0.7	267	1870	7.0	0.1~0.9	34	0.5	0.9	6.0	0.4	12.7	79.5
1952美国高尔加斯	45	0.5	113	2110	19	2.7	352	7.1	7.6	11.7	2.1	0.6	70.9
1978美国汉纳	62	1.1	230	2040	8.9	8.4	757	1.9	25.1	44.0	10.1	0	16.1
1979比利时布阿略达姆	87	1.4	365	2500	6.8	8.5	1500	18.5	36.1	36.1	5.4	0.1	0
1979比利时布阿略达姆	101	2.1	519	1950	3.8	9.7	1385	36.2	31.8	31.8	3.0	0.1	2.0
1952苏联顿巴斯	85	1.4	356	3080	8.7	4.2	1001	15.9	14.8	12.1	1.8	0.2	54.8
1956苏联莫斯科近郊	66	1.5	286	2900	10.1	3.5	658	7.1	14.1	19.5	1.5	0.3	55.9
1950英国纽门斯平尼	27.5	0.4	63	300	4.8	2.1	41	4.9	7.9	15.5	1.0	0	70.7
1994中国徐州新河	168	2.6	960	3240	3.4	13.1	2657^①	12.2	58.0	14.6	11.9	0	3.3
1996中国唐山刘庄	110/200	3.4	1319/ 2638	2325	1.8	12.5	1674	14.0	46.0	17.0	12.0		10.0
1996中国唐山刘庄	110/200	3.4	1319/ 2638	4583	3.5	5.0	1627	15.0	15.0	13.5	3.0		52.5
1996中国山东新汶	63/74			1357		10.1	841	9.4	44.1	30.0	8.5	0.7	7.9
2007中国乌兰察布				6250
2010中国甘肃华亭				3067		4.1	938	12.7	16.3	17.5	1.5	0	51.7
				3216		4.8	1141	13.9	19.6	15.5	2.0	0	48.7
				3408		5.6	1388	18.0	20.6	19.0	2.1	0	39.8
				2096		6.7	1043	22.1	25.4	21.2	2.3	0	28.6
				1140		9.3	790	29.6	36.2	25.7	3.5	0	4.5

试验年份和地点	气化通道尺寸			粗煤气产出			有效气产量/ (m³/h)	产气组成/%（有些总和不是100%）
试验年份和地点	长度/ m	断面/ m²	气化面/ m²	产量/ (m³/h)	速率/ (m/h)	热值/ (MJ/m³)	有效气产量/ (m³/h)	CO	H₂	CO₂	CH₄	O₂	N₂
1948美国高尔加斯	90	0.7	267	1870	7.0	0.1~0.9	34	0.5	0.9	6.0	0.4	12.7	79.5
1952美国高尔加斯	45	0.5	113	2110	19	2.7	352	7.1	7.6	11.7	2.1	0.6	70.9
1978美国汉纳	62	1.1	230	2040	8.9	8.4	757	1.9	25.1	44.0	10.1	0	16.1
1979比利时布阿略达姆	87	1.4	365	2500	6.8	8.5	1500	18.5	36.1	36.1	5.4	0.1	0
1979比利时布阿略达姆	101	2.1	519	1950	3.8	9.7	1385	36.2	31.8	31.8	3.0	0.1	2.0
1952苏联顿巴斯	85	1.4	356	3080	8.7	4.2	1001	15.9	14.8	12.1	1.8	0.2	54.8
1956苏联莫斯科近郊	66	1.5	286	2900	10.1	3.5	658	7.1	14.1	19.5	1.5	0.3	55.9
1950英国纽门斯平尼	27.5	0.4	63	300	4.8	2.1	41	4.9	7.9	15.5	1.0	0	70.7
1994中国徐州新河	168	2.6	960	3240	3.4	13.1	2657^①	12.2	58.0	14.6	11.9	0	3.3
1996中国唐山刘庄	110/200	3.4	1319/ 2638	2325	1.8	12.5	1674	14.0	46.0	17.0	12.0		10.0
1996中国唐山刘庄	110/200	3.4	1319/ 2638	4583	3.5	5.0	1627	15.0	15.0	13.5	3.0		52.5
1996中国山东新汶	63/74			1357		10.1	841	9.4	44.1	30.0	8.5	0.7	7.9
2007中国乌兰察布				6250
2010中国甘肃华亭				3067		4.1	938	12.7	16.3	17.5	1.5	0	51.7
				3216		4.8	1141	13.9	19.6	15.5	2.0	0	48.7
				3408		5.6	1388	18.0	20.6	19.0	2.1	0	39.8
				2096		6.7	1043	22.1	25.4	21.2	2.3	0	28.6
				1140		9.3	790	29.6	36.2	25.7	3.5	0	4.5

气化炉		单台规模			产气组成/%（有些总和不是100%）
气化炉		煤量/(t/d)	粗气/(m³/h)	有效气/(m³/h)	CO	H₂	CO₂	CH₄	O₂	N₂
气流床（1400~1600℃）	多喷嘴对置^[10]	3000 4000	—	200000 247500	45.5	35.5	18.5	—	—	—
	GE^[11]		—	—	43.9	37.0	19.5	—	—	—
	航天炉^[10]	3500	—	—	67.5	25.0	5.5	—	—	—
	壳牌^[12-13]	3000	—	—	63.3	21.1	13.8	—	—	1.8
	GSP^[11-12]	2000	—	—	58.9	29.1	5.6	—	—	—
	西安热工两段^[13]	2000	—	—	51.0	31.2	17.8	—	0.1	—
流化床（800~1000℃）	中科院工热所^[10]	2500	200000	—	—	—	—	—	—	—
	循环流化床^[14]	700~1000	80000	—	—	—	—	—	—	—
	灰熔聚-瘦煤^[15]		—	—	26.7	42.1	21.0	1.9	—	8.2
	灰熔聚-长焰煤^[15]		—	—	29.5	39.7	21.6	1.7	—	7.4
	流化床^[10]	—	—	—	41.5	38.5	15.0	—	—	—
移动床（固态排渣和液态排渣的温度不同，气化区温度800~1400℃）	碎煤加压固态排渣^[10]	1500	—	119,000	25	38.5	22.5	10.5	—	—
	碎煤加压-义马	—	110000	—	—	—	—	—	—	—
	鲁奇Mark V固渣	2000	100000~140000	—	—	—	—	—	—	—
	Mark+^[16]	—	120000	—	—	—	—	—	—	—
	鲁奇无烟煤^[15]	—	—	—	20.3	45.3	27.5	4.7	—	1.3
	鲁奇次烟煤^[15]	—	—	—	21.4	38.4	28.9	9.6	—	1.0
	鲁奇褐煤^[15]	—	—	—	19.1	37.2	30.7	11.8	—	0.5

气化炉		单台规模			产气组成/%（有些总和不是100%）
气化炉		煤量/(t/d)	粗气/(m³/h)	有效气/(m³/h)	CO	H₂	CO₂	CH₄	O₂	N₂
气流床（1400~1600℃）	多喷嘴对置^[10]	3000 4000	—	200000 247500	45.5	35.5	18.5	—	—	—
	GE^[11]		—	—	43.9	37.0	19.5	—	—	—
	航天炉^[10]	3500	—	—	67.5	25.0	5.5	—	—	—
	壳牌^[12-13]	3000	—	—	63.3	21.1	13.8	—	—	1.8
	GSP^[11-12]	2000	—	—	58.9	29.1	5.6	—	—	—
	西安热工两段^[13]	2000	—	—	51.0	31.2	17.8	—	0.1	—
流化床（800~1000℃）	中科院工热所^[10]	2500	200000	—	—	—	—	—	—	—
	循环流化床^[14]	700~1000	80000	—	—	—	—	—	—	—
	灰熔聚-瘦煤^[15]		—	—	26.7	42.1	21.0	1.9	—	8.2
	灰熔聚-长焰煤^[15]		—	—	29.5	39.7	21.6	1.7	—	7.4
	流化床^[10]	—	—	—	41.5	38.5	15.0	—	—	—
移动床（固态排渣和液态排渣的温度不同，气化区温度800~1400℃）	碎煤加压固态排渣^[10]	1500	—	119,000	25	38.5	22.5	10.5	—	—
	碎煤加压-义马	—	110000	—	—	—	—	—	—	—
	鲁奇Mark V固渣	2000	100000~140000	—	—	—	—	—	—	—
	Mark+^[16]	—	120000	—	—	—	—	—	—	—
	鲁奇无烟煤^[15]	—	—	—	20.3	45.3	27.5	4.7	—	1.3
	鲁奇次烟煤^[15]	—	—	—	21.4	38.4	28.9	9.6	—	1.0
	鲁奇褐煤^[15]	—	—	—	19.1	37.2	30.7	11.8	—	0.5

项目	地下气化^①	移动床	流化床	气流床
颗粒直径d/10^-3 m	700	10	4	0.02
等质量煤颗粒数之比	—	1	15.6	1250000
等质量煤颗粒表面积A之比	0.014	1	2.5	500
气化炉中煤颗粒的停留时间/s	—	3600	1200~1800	5~10
气化炉中瞬时煤质量的表面积比	0.014	1	0.8~1.3	0.7~1.4