CN106497606A - 煤直接加氢热解方法 - Google Patents
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Abstract
本发明涉及到一种煤直接加氢热解方法,来自磨煤装置的煤粉通过煤粉输送装置送至气化炉的气化喷嘴和粉煤喷嘴,由汽包产生的蒸汽和从界区来的氧气与煤粉一起经由气化喷嘴进入气化室反应,产生高温富氢合成气和煤渣;煤渣沿下降管进入激冷室内,合成气经由各喷孔进入热解室,与来自粉煤烧嘴的煤粉反应,生成的油气和煤焦进入旋风分离器分离出煤焦和油气;油气与锅炉水换热后进入油气分离装置,分离出油品和可燃气体;可燃气体进入气体净化装置,分离出合成气和燃料气,燃料气送去磨煤单元;换热后的锅炉水进入气化炉的冷壁,吸收热量后生成汽水混合物,汽水混合物进入汽包,分离蒸汽和水,蒸汽送去气化喷嘴。
Description
技术领域
本发明涉及到煤化工,具体指一种煤直接加氢热解方法。
背景技术
煤直接加氢工艺过程主要包括煤的破碎与干燥、煤浆制备、加氢液化、固液分离、气体净化、液体产品分馏和精制以及制氢等部分。主要流程为:在高温高压下,高浓度煤浆中的煤发生热解,在催化剂作用下进行加氢和分解,最终成为稳定的液体分子。液化过程中,将煤、催化剂和循环油制成的煤浆,与制得的氢气混合送入反应器。在液化反应器内,煤首先发生热解反应,生成自由基“碎片”,不稳定的自由基“碎片”再与氢在催化剂存在条件下结合,形成分子量比煤低得多的初级加氢产物。出反应器的产物构成十分复杂,包括气、液、固三相。气相的主要成分是氢气,分离后循环返回反应器重新参加反应;固相为未反应的煤、矿物质及催化剂;液相则为轻油(粗汽油)、中油等馏份油及重油。液相馏份油经提质加工(如加氢精制、加氢裂化和重整等)得到合格的汽油、柴油和航空煤油等产品。重质的液固淤浆经进一步分离得到重油和残渣,重油作为循环溶剂用于煤浆制备。
现有的煤直接液化技术中,反应器反应压力高达17MPa-30Mpa,氢耗量高达6%-10%,流程复杂,投资成本高。工艺过程中不仅要补充大量新氢,还需要循环油作供氢溶剂,装置生产能力降低,出液化反应器的产物组成复杂,固液两相分离困难,产油率低。
发明内容
本发明所要解决的技术问题是针对现有技术的现状提供一种集煤制氢和煤加氢一体化、无需配套煤制氢装置且反应条件温和、氢耗量小、产油率高的煤直接加氢方法。
本发明解决上述技术问题所采用的技术方案为:该煤直接加氢热解方法,其特征在于包括下述步骤:
来自磨煤装置的煤粉通过煤粉输送装置送至气化炉的气化喷嘴和粉煤喷嘴,其中,粉煤输送混合相流速为4~15m/s;混合密度为200~550kg/m3;
由汽包产生的蒸汽和从界区来的氧气与煤粉一起经由气化喷嘴进入气化室反应,产生高温富氢合成气和煤渣;控制蒸汽、氧气和煤粉的比例为0.2~0.8Nm3氧气/kg煤,0.1~0.5Nm3蒸汽/Nm3氧气;控制气化室内反应温度为600~1500℃,压力为1.0~6.0MPag;
煤渣和合成气进入下降管;煤渣在自身重力作用下沿下降管进入激冷室内,冷却后排出;
合成气上行,经由各喷孔进入热解室内,与来自粉煤烧嘴的煤粉反应,生成油气和煤焦;控制所述热解室内的反应温度为600~1200℃、压力为1.0~6.0MPag;
所述油气和煤焦从出料口排出,进入旋风分离器内分离出煤焦和油气;
分离后的煤焦从所述旋风分离器的底部出口排出;分离出的油气则从旋风分离器的顶部出口排出,与锅炉水换热后进入油气分离装置,分离出油品和以CO、H2和CH4为主要成分的可燃气体;
所述可燃气体进入气体净化装置,分离出合成气和燃料气,燃料气送去磨煤单元;
换热后的锅炉水进入所述气化炉的冷壁,吸收热量后生成汽水混合物,汽水混合物进入汽包,分离蒸汽和水,所述蒸汽送去所述气化喷嘴。
优选所述煤粉的粒径小于等于90微米,含水量小于等于2wt%,煤粉的温度为80~100℃。
所述煤粉输送装置为气力输送装置。
优选所述旋风分离为两级旋风分离。
作为优选,上述各方案中的气化炉的顶部设有气化喷嘴,所述气化炉的内腔自上而下依次设有气化室、热解室和激冷室,下降管的上端口连接所述气化室的底部出口,所述下降管的下端口穿过所述热解室***到所述激冷室内;所述气化炉的底部设有渣出口;
所述下降管的顶部入口通过挡板密封连接所述气化室的外侧壁;所述挡板上间隔设有多个对向所述热解室喷孔;
所述气化炉的侧壁上设有至少一个对向所述热解室的粉煤喷嘴;所述气化炉的侧壁上还设有连通所述热解室的物料出口。
所述挡板与所述气化炉的轴向夹角为15~60°。
所述粉煤喷嘴的轴向与所述气化炉(1)的径向夹角为0~60°,以使煤粉与合成气充分接触,提高反应效率。
所述热解室的底面相对于所述气化炉的侧壁倾斜设置,所述物料出口设置在所述热解室的最低位置。
所述粉煤喷嘴有多个,沿所述气化炉的周壁均匀布置。
与现有技术相比,本发明所提供是煤直接加氢热解方法,将煤制氢和煤热解集成在一个反应器中实现了煤制氢和煤加氢的一体化,无需配套煤制氢装置;且反应条件温和,不需要外供氢源,氢耗量小,只有2%左右,产油率高,设备投资省;并且需催化剂,操作运行费用低;
主要反应在1~3秒内完成,反应器处理能力大;
气化室与热解室为水冷壁结构,通过回收气化反应与热解加氢反应的大部分热量,产生大量蒸汽减少能耗;通过废锅回收合成气部分热量,提高了热能利用率;节能降耗效果好;
油气分离装置与气体净化装置分离出燃料气供磨煤装置使用,实现了物料的循环利用,提高了整套装置的效率。
附图说明
图1为本发明实施例流程示意图;
图2为本发明实施例中气化炉的放大图;
图3为本发明实施例中气化喷嘴的剖视示意图;
图4为本发明实施例中粉煤喷嘴的剖视示意图;
图5为本发明实施例粉煤喷嘴布置示意图。
具体实施方式
以下结合附图实施例对本发明作进一步详细描述。
如图1至图5所示,本实施例中使用的主要反应器是气化炉1,气化炉1的顶部设有气化喷嘴2,气化炉的底部设有渣出口14;气化炉的内腔自上而下依次分为气化室11、热解室15和激冷室13。
其中,热解室15的底面相对于气化炉1的侧壁倾斜设置;气化炉1的侧壁上设有连通热解室15的物料出口17,物料出口17设置在热解室15的最低位置处,以方便出料。
气化室11的底部为锥形结构,其底部出口16为外扩的上小下大的喇叭口,底部出口连通下降管12并容置在挡板4。
下降管12,连接气化室11和激冷室13,为渣料的下降通道;其下端口穿过热解室15底面***到激冷室的液面内;下降管12的顶部入口通过挡板4密封连接气化室11的外侧壁。
本实施例中,挡板4与气化炉1的轴向夹角为45°挡板4上间隔设有多个对向热解室15的喷孔41。
激冷室13,用于对反应所产生的渣料进行冷却后排出气化炉,下降管12连接有激冷装置(图中未示出),用于冷却保护下降管,同时向激冷室提供冷却水;激冷室的侧壁上还设有激冷水通道18,用于向激冷室内补水,保持激冷室内液位。
本实施例中的激冷装置可根据需要选用现有技术中的任意一种。
气化喷嘴2,用于向气化室内喷送反应物料,可根据需要选用现有技术中的任意一种。本实施例中的气化喷嘴2包括第一本体,第一本体上由内而外依次设有燃料通道22、氧气通道23、蒸汽通道24和第一冷却通道25;燃料通道22与所述氧气通道23之间的隔层26采用耐磨材料制备。
粉煤喷嘴3,有八个,均布在气化炉的周向侧壁上,其出口对向热解室15,用于向热解室15内喷射煤粉;包括第二本体31,第二本体31上设有粉煤通道32,粉煤通道32外设有第二冷却通道33。第二本体31采用耐磨材料制备。
本实施例中,粉煤喷嘴3的轴向与气化炉1的径向夹角为60°,与气化室的底部锥面相平行。
来自磨煤装置8的粒径小于等于90微米、含水量小于等于2wt%//温度为80~100℃的煤粉通过煤粉输送装置9送至气化炉1的气化喷嘴2和粉煤喷嘴3,其中,粉煤输送混合相流速为10m/s;混合密度为350kg/m3;所述煤粉输送装置9为气力输送装置,输送气体为氮气,输送压力为4.0MPag。
由汽包10产生的蒸汽和从界区来的氧气与煤粉一起经由气化喷嘴2进入气化室11反应,生成以CO+H2为主要组成的高温富氢合成气和煤渣;控制蒸汽、氧气和煤粉的比例为0.50Nm3氧气/kg煤,蒸汽量可取0.3Nm3/Nm3氧气;控制气化室内反应温度为600~1500℃,压力为1.0~6.0MPag;
煤渣和合成气进入下降管12;煤渣在自身重力作用下沿下降管12进入激冷室13内,冷却后排出;控制激冷室的温度在300℃以下。
合成气上行,经由各喷孔41进入热解室15内,与来自粉煤烧嘴3的煤粉反应,生成油气和煤焦;控制所述热解室15内的反应温度为800~900℃、压力为3.5±0.2MPag;
所述油气和煤焦从出料口17排出,依次进入两级旋风分离器5内分离出煤焦和油气;
分离后的煤焦从所述旋风分离器5的底部出口排出;分离出的油气则从旋风分离器5的顶部出口排出,与锅炉水换热后进入油气分离装置6,分离出油品和以CO、H2和CH4为主要成分的可燃气体;
可燃气体进入气体净化装置7,分离出合成气和燃料气,燃料气送去磨煤单元8;
换热后的锅炉水进入所述气化炉1的冷壁,吸收热量后生成汽水混合物,汽水混合物进入汽包,分离蒸汽和水,蒸汽送去所述气化喷嘴2。
本发明中能效可达70~80%,现有技术中煤炭直接液化技术的能效仅约50%;煤耗为3.3~3.5吨,低于现有煤炭直接液化技术;液相产品收率可达25~33%,与现有先进水平持平;CO2排放量0.05~0.5吨/吨油品,比现有煤炭直接液化技术5~6吨/吨油品明显减少,百万吨级别投资为现有煤炭直接液化技术的50~60%。
综合技术指标、环保指标及投资方面,本发明相比现有技术均具有明显的优势。
Claims (9)
1.煤直接加氢热解方法,其特征在于包括下述步骤:
来自磨煤装置(8)的煤粉通过煤粉输送装置(9)送至气化炉(1)的气化喷嘴(2)和粉煤喷嘴(3),其中,粉煤输送混合相流速为4~15m/s;混合密度为200~550kg/m3;
由汽包(10)产生的蒸汽和从界区来的氧气与煤粉一起经由气化喷嘴(2)进入气化室(11)反应,产生高温富氢合成气和煤渣;控制蒸汽、氧气和煤粉的比例为0.2~0.8Nm3氧气/kg煤,0.1~0.5Nm3蒸汽/Nm3氧气;气化室内反应温度为600~1500℃,压力为1.0~6.0MPag;
煤渣和合成气进入下降管(12);煤渣在自身重力作用下沿下降管(12)进入激冷室(13)内,冷却后排出;
合成气上行,经由各喷孔(41)进入热解室(15)内,与来自粉煤烧嘴(3)的煤粉反应,生成油气和煤焦;控制所述热解室(15)内的反应温度为600~1200℃、压力为1.0~6.0MPag;
所述油气和煤焦从出料口(17)排出,进入旋风分离器(5)内分离出煤焦和油气;
分离后的煤焦从所述旋风分离器(5)的底部出口排出;分离出的油气则从旋风分离器(5)的顶部出口排出,与锅炉水换热后进入油气分离装置(6),分离出油品和以CO、H2和CH4为主要成分的可燃气体;
所述可燃气体进入气体净化装置(7),分离出合成气和燃料气,燃料气送去磨煤单元(8);
换热后的锅炉水进入所述气化炉(1)的冷壁,吸收热量后生成汽水混合物,汽水混合物进入汽包,分离蒸汽和水,所述蒸汽送去所述气化喷嘴(2)。
2.根据权利要求1所述的煤直接加氢热解方法,其特征在于所述煤粉的粒径小于等于90微米,含水量小于等于2wt%,煤粉的温度为80~100℃。
3.根据权利要求1或2所述的煤直接加氢热解方法,其特征在于所述煤粉输送装置(9)为气力输送装置。
4.根据权利要求3所述的煤直接加氢热解方法,其特征在于所述旋风分离为两级旋风分离。
5.根据权利要求1至4任一权利要求所述的煤直接加氢热解方法,其特征在于所述气化炉(1)的顶部设有气化喷嘴(2),所述气化炉的内腔自上而下依次设有气化室(11)、热解室(15)和激冷室(13),下降管(12)的上端口连接所述气化室(11)的底部出口,所述下降管(12)的下端口穿过所述热解室(15)***到所述激冷室(13)内;所述气化炉(1)的底部设有渣出口(14);
所述下降管(12)的顶部入口通过挡板(4)密封连接所述气化室(11)的外侧壁;所述挡板(4)上间隔设有多个对向所述热解室(15)喷孔(41);
所述气化炉(1)的侧壁上设有至少一个对向所述热解室(15)的粉煤喷嘴(3);所述气化炉(1)的侧壁上还设有连通所述热解室(15)的物料出口(17)。
6.根据权利要求5所述的煤直接加氢热解方法,其特征在于所述挡板(4)与所述气化炉(1)的轴向夹角为15~60°。
7.根据权利要求6所述的煤直接加氢热解方法,其特征在于所述粉煤喷嘴(3)的轴向与所述气化炉(1)的径向夹角为0~60°。
8.根据权利要求7所述的煤直接加氢热解方法,其特征在于所述热解室(15)的底面相对于所述气化炉(1)的侧壁倾斜设置,所述物料出口(17)设置在所述热解室(15)的最低位置。
9.根据权利要求8所述的煤直接加氢热解方法,其特征在于所述粉煤喷嘴(3)有多个,沿所述气化炉的周壁均匀布置。
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