CN113980708A - 一种超高co2含量合成气脱碳方法 - Google Patents
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Abstract
本发明属于煤炭地下气化技术领域,具体涉及一种超高CO2含量合成气脱碳方法,将CO2吸收塔下部的富胺溶液通过富胺闪蒸罐的闪蒸,以及胺再生塔的再生后将贫胺溶液通入CO2吸收塔的上部进行再次循环利用,将富胺闪蒸罐闪蒸后的溶液通入到CO2吸收塔的中部进行预吸收,预吸收后的原料天然气再与再生后的贫胺液在CO2吸收塔上半段接触,从而使原料天然气中的酸性组分达到处理指标要求。本发明解决了脱碳过程中能耗高的问题,具有利于胺溶液循环使用、再生能耗低的优点。
Description
技术领域
本发明属于煤炭地下气化技术领域,具体涉及一种超高CO2含量合成气脱碳方法。
背景技术
煤炭地下气化技术是将处于地下的煤炭进行有控制的燃烧,通过对煤层的热作用及化学作用而产生可燃气体(主要成分为H2、CO、CO2、CH4等)的过程,该过程集建井、采煤、地面气化三大工艺为一体,变传统的物理采煤为化学采煤。煤炭地下气化技术不仅可以回收矿井遗弃煤炭资源,而且还可以用于开采井工难以开采或开采经济性、安全性较差的薄煤层、深部煤层、“三下”压煤和高硫、高灰、高瓦斯煤层;地下气化灰渣留在气化区,减少了地表下沉,无固体物质排放,煤气可以集中净化,大大减少了煤炭开采和使用过程中对环境的破坏,因具有安全性好、投资少、效益高、污染少等优点,深受世界各国的重视,是煤炭开采利用技术的重要补充。
现有的煤制气预处理工艺通常采用的是低温甲醇洗技术,即以甲醇为吸收剂,在低温条件下H2S、COS、CO2等酸性气体在甲醇中溶解度大的物理特性。但由于地下煤合成气中CO2等含量超过50%,不满足甲醇洗工艺要求。由于合成气中CO2含量约50%,几乎达到传统MDEA脱碳工艺的上限(55%),设备较大,选型难,且再生能耗超高。
发明内容
本发明的目的是克服现有技术的不足而提供一种超高CO2含量合成气脱碳方法,可以大幅度降低胺液的循环量和再生塔的再生负荷。
本发明的技术方案如下:
一种超高CO2含量合成气脱碳方法,所述方法包括如下步骤:
(1)预制煤合成气经过预处理单元形成原料天然气,原料天然气通入过滤器内将粒径大于10μm的液体及杂质除去,将过滤后的原料天然气通入CO2吸收塔下部,所述CO2吸收塔内设有自塔顶流向塔底的贫胺溶液,贫胺溶液与原料天然气逆向接触后将原料天然气中的CO2吸收形成净化气,贫胺溶液吸收CO2后形成富胺溶液;
(2)CO2吸收塔的顶部设置有净化气冷却器将净化气冷却,净化气冷却器连通有净化气分离器将净化气分离后通入脱水工艺进行后续生产工艺;
(3)CO2吸收塔的底部连通有富胺闪蒸罐,塔底的富胺溶液进入富胺闪蒸罐,富胺溶液经闪蒸后形成闪蒸气和半贫液;
(4)所述富胺闪蒸罐下端连通有三通阀将半贫液分成两股,所述三通阀的其中一个输出口和胺再生塔连通,所述三通阀的另一个输出口通过连接管道连通有第一增压泵,所述第一增压泵的输出口通过连接管道和所述CO2吸收塔的中部连通,通入CO2吸收塔的中部的半贫液对原料天然气进行预吸收。
(5)富胺闪蒸罐和胺再生塔之间设置有换热器,所述半贫液经过换热器的换热后通入胺再生塔,将胺液中的CO2脱除;
(6)所述胺再生塔的塔顶设置有塔顶冷却器和塔顶回流罐,胺再生塔内的气体冷却后通入放空系统,冷却后形成的液体经由塔顶回流罐回流至胺再生塔内;
(7)所述胺再生塔的塔底连通有重沸器,将胺再生塔塔底的胺液加热,重沸器加热产生的气体返回胺再生塔,重沸器加热后的胺液为贫胺液,所述贫胺液经过所述换热器的换热后通入贫胺缓冲罐;
(8)所述贫胺缓冲罐连通至CO2吸收塔顶部开始新的循环。
进一步地,所述富胺闪蒸罐的上端连通有闪蒸气分离器,所述富胺闪蒸罐和闪蒸气分离器之间设置有闪蒸气冷却器,所述闪蒸器分离器连通有第一混合器,所述塔顶回流罐连通至所述第一混合器,第一混合器将闪蒸气和步骤(6)中冷却后的气体混合后通入放空系统。
进一步地,所述富胺闪蒸罐和换热器之间设置有预加热器。
进一步地,步骤(6)中塔顶冷却器的冷却温度为65℃。
进一步地,步骤(7)中的重沸器的加热温度为109℃。
进一步地,所述胺再生塔上设置有液位报警器,用以方便补充胺再生塔内的胺溶液量。
进一步地,所述胺再生塔上设置有压力调节阀,用以控制胺再生塔顶部压力。
与现有技术相比,本发明的有益效果是:
1、本发明通过设置有富胺闪蒸罐和胺再生塔将CO2吸收塔除碳后的富胺溶液进行回收再利用,胺溶液的循环利用有效避免了浪费,降低了成本。
2、本发明通过将半贫液设置为两股,其中一股通入再生塔再生,另一股通入CO2吸收塔中部,对原料天然气先进行预吸收,预吸收后的原料天然气再与再生后的贫胺液在CO2吸收塔上半段接触,从而使原料天然气中的酸性组分达到处理指标要求,增加预吸收后有效提升除碳效果,有效降低胺溶液的循环量和再生塔的再生负荷,从而有效降低胺溶液的再生能耗,使再生能耗由240MW降低至80MW左右,装置能耗下降70%以上。
总之,本发明具有利于胺溶液循环使用、再生能耗低的优点。
附图说明
图1为本发明的工艺流程图;
图2为本发明中CO2吸收塔和胺再生塔的操作参数表。
图中,Q1、过滤器,T1、CO2吸收塔,V1、富胺闪蒸罐,E1、预加热器,L1、换热器,T2、胺再生塔,ACl、半贫液冷却器,AC2、塔顶冷却器,V4、塔顶回流罐,AC4、净化气冷却器,V2、净化气分离器,AC5、闪蒸气冷却器,V3、闪蒸气分离器,P1、第一增压泵,P2、第二增压泵,H1、第一混合器,H2、第二混合器,F1、重沸器,AC3、贫胺液冷却器。
具体实施方式
下面将结合本发明实施例中的附图,对本发明实施例中的技术方案进行清楚、完整地描述,显然,所描述的实施例仅仅是本发明一部分实施例,而不是全部的实施例。基于本发明中的实施例,本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施例,都属于本发明保护的范围。
如图1-2所示,一种超高CO2含量合成气脱碳方法,所述方法包括如下步骤:
(1)预制煤合成气经过预处理单元形成原料天然气,原料天然气通入过滤器Q1内将粒径大于10μm的液体及杂质除去,将过滤后的原料天然气通入CO2吸收塔T1下部,过滤后的原料天然气进入CO2吸收塔T1的流量为56780m3/h、压力为3.35MPa、温度为42℃,所述CO2吸收塔T1内设有自塔顶流向塔底的贫胺溶液,贫胺溶液进入CO2吸收塔T1的流量为297000kg/h、压力为3.5MPa、温度为40℃,贫胺溶液与原料天然气逆向接触后将原料天然气中的CO2吸收形成净化气,净化气的二氧化碳浓度不超过50ppm,出塔温度为40℃,贫胺溶液吸收CO2后形成富胺溶液,富胺溶液的出塔温度为85℃;
其中,贫胺溶液由重量份31.48%的MDEA、59.86%的水、8.66%的哌嗪组成,MDEA溶液简称胺液,该工艺具有酸气负荷大、二氧化碳脱除效率高的优点,可将原料气中二氧化碳含量脱除至50ppm以下;
(2)CO2吸收塔T1的顶部设置有净化气冷却器AC4将净化气冷却,净化气冷却器AC4连通有净化气分离器V2将净化气分离后通入脱水工艺进行后续生产工艺;
(3)CO2吸收塔T1的底部连通有富胺闪蒸罐V1,塔底的富胺溶液进入富胺闪蒸罐V1,富胺溶液经闪蒸后形成闪蒸气和半贫液,富胺闪蒸罐V1内的压力为0.13MPa;
(4)所述富胺闪蒸罐V1下端连通有三通阀将半贫液分成两股,所述三通阀的其中一个输出口和胺再生塔T2连通,所述三通阀的另一个输出口通过连接管道连通有第一增压泵P1,所述第一增压泵P1的输出口通过连接管道和所述CO2吸收塔T1的中部连通,第一增压泵P1和CO2吸收塔T1之间设置有半贫液冷却器AC1,将半贫液冷却后通入CO2吸收塔T1的中部的半贫液对原料天然气进行预吸收,由于原料天然气从CO2吸收塔T1的下部通入,位于CO2吸收塔T1下半段的原料天然气的酸性组分浓度较高,CO2吸收塔T1下半段的原料天然气进行预吸收,经过预吸收后的原料天然气再与再生后的贫胺液在CO2吸收塔T1上半段接触,从而使原料天然气中的酸性组分达到处理指标要求,增加预吸收后可有效提升除碳效果,有效降低胺溶液的循环量和再生塔的再生负荷,从而有效降低胺溶液的再生能耗,使再生能耗由240MW降低至80MW左右,装置能耗下降70%以上。
(5)富胺闪蒸罐V1和胺再生塔T2之间设置有换热器L1,所述半贫液经过换热器L1的换热后通入胺再生塔T2,将胺液中的CO2脱除,半贫液进入胺再生塔T2的温度为100℃,此时,胺再生塔T2塔顶的压力为0.005MPa、温度为97.6℃,胺再生塔T2塔底的压力为0.01MPa、温度为113.5℃;
(6)所述胺再生塔T2的塔顶设置有塔顶冷却器AC2和塔顶回流罐V4,胺再生塔T2内的气体经过冷却后通入放空系统,冷却后形成的液体经由塔顶回流罐V4回流至胺再生塔T2内;
(7)所述胺再生塔T2的塔底连通有重沸器F1,将胺再生塔T2塔底的胺液加热,重沸器F1加热产生的气体返回胺再生塔T2,重沸器F1加热后的胺液为贫胺液,所述贫胺液经过所述换热器L1的换热后通入贫胺缓冲罐;
(8)所述贫胺缓冲罐连通至CO2吸收塔T1顶部开始新的循环,所述贫胺缓冲罐和CO2吸收塔T1之间设置有贫胺液冷却器AC3对贫胺液进行冷却,在贫胺液冷却器AC3和CO2吸收塔之间设置有第二混合器H2,将冷却后的贫胺液通入第二混合器H2内,将步骤(2)中净化气分离器V2分离净化气后的含胺溶液通入第二混合器H2中,将闪蒸气分离器V3中分离闪蒸气后的含胺溶液通入至第二混合器H2中,步骤(6)中胺再生塔T2冷却后产生的含胺溶液分成两股,其中一股回流至胺再生塔T2内,另一股通入第二混合器H2内和将冷却后的贫胺液混合,混合后在通过抽料泵将混合后的贫胺液通入至CO2吸收塔T1的塔顶。
本实施例中,所述富胺闪蒸罐V1的上端连通有闪蒸气分离器V3,所述富胺闪蒸罐V1和闪蒸气分离器V3之间设置有闪蒸气冷却器AC5,所述闪蒸器分离器V3连通有第一混合器H1,所述塔顶回流罐V4连通至所述第一混合器H1,第一混合器H1将闪蒸气和步骤(6)中冷却后的气体混合后通入放空系统。
本实施例中,所述富胺闪蒸罐V1和换热器L1之间设置有预加热器E1,对分流至胺再生塔T2内的半贫液进行预加热,避免换热器L1的效果不足,从而避免影响生产,在富胺闪蒸罐V1和预加热器E1之间设置有第二增压泵P2对半贫液进行增压。
本实施例中,步骤(6)中塔顶冷却器AC2的冷却温度为65℃。
本实施例中,步骤(7)中的重沸器F1的加热温度为109℃。
本实施例中,所述胺再生塔T2上设置有液位报警器,用以方便补充胺再生塔T2内的胺溶液量,从而利于调节脱碳工艺系统中的胺溶液量的调节,在胺溶液含量不足时能够及时补充。
本实施例中,所述胺再生塔T2上设置有压力调节阀,用以控制胺再生塔T2顶部压力,以维持胺再生塔T2顶部的压力在生产所需的范围内。
本实施例中,为防止MDEA溶液发泡,系统中需增加消泡剂罐、胺过滤器以及新鲜MDEA补充装置,只有当MDEA溶液发泡时才向系统内通入少量消泡剂。
尽管参照前述实施例对本发明进行了详细的说明,对于本领域的技术人员来说,其依然可以对前述各实施例所记载的技术方案进行修改,或者对其中部分技术特征进行等同替换,凡在本发明的精神和原则之内,所作的任何修改、等同替换、改进等,均应包含在本发明的保护范围。
Claims (7)
1.一种超高CO2含量合成气脱碳方法,其特征在于:所述方法包括如下步骤:
(1)预制煤合成气经过预处理单元形成原料天然气,原料天然气通入过滤器内将粒径大于10μm的液体及杂质除去,将过滤后的原料天然气通入CO2吸收塔下部,所述CO2吸收塔内设有自塔顶流向塔底的贫胺溶液,贫胺溶液与原料天然气逆向接触后将原料天然气中的CO2吸收形成净化气,贫胺溶液吸收CO2后形成富胺溶液;
(2)CO2吸收塔的顶部设置有净化气冷却器将净化气冷却,净化气冷却器连通有净化气分离器将净化气分离后通入脱水工艺进行后续生产工艺;
(3)CO2吸收塔的底部连通有富胺闪蒸罐,塔底的富胺溶液进入富胺闪蒸罐,富胺溶液经闪蒸后形成闪蒸气和半贫液;
(4)所述富胺闪蒸罐下端连通有三通阀将半贫液分成两股,所述三通阀的其中一个输出口连通有胺再生塔,所述三通阀的另一个输出口通过连接管道连通有第一增压泵,所述第一增压泵的输出口通过连接管道和所述CO2吸收塔的中部连通,通入CO2吸收塔的中部的半贫液对原料天然气进行预吸收;
(5)富胺闪蒸罐和胺再生塔之间设置有换热器,所述半贫液经过换热器的换热后通入胺再生塔,将胺液中的CO2脱除;
(6)所述胺再生塔的塔顶设置有塔顶冷却器和塔顶回流罐,胺再生塔内的气体经过冷却后通入放空系统,冷却后形成的液体经由塔顶回流罐回流至胺再生塔内;
(7)所述胺再生塔的塔底连通有重沸器,将胺再生塔塔底的胺液加热,重沸器加热产生的气体返回胺再生塔,重沸器加热后的胺液为贫胺液,所述贫胺液经过所述换热器的换热后通入贫胺缓冲罐;
(8)所述贫胺缓冲罐连通至CO2吸收塔顶部开始新的循环。
2.根据权利要求1所述的超高CO2含量合成气脱碳方法,其特征在于:所述富胺闪蒸罐的上端连通有闪蒸气分离器,所述富胺闪蒸罐和闪蒸气分离器之间设置有闪蒸气冷却器,所述闪蒸器分离器连通有第一混合器,所述塔顶回流罐连通至所述第一混合器,第一混合器将闪蒸气和步骤(6)中冷却后的气体混合后通入放空系统。
3.根据权利要求1所述的超高CO2含量合成气脱碳方法,其特征在于:所述富胺闪蒸罐和换热器之间设置有预加热器。
4.根据权利要求1所述的超高CO2含量合成气脱碳方法,其特征在于:步骤(6)中塔顶冷却器的冷却温度为65℃。
5.根据权利要求1所述的超高CO2含量合成气脱碳方法,其特征在于:步骤(7)中的重沸器的加热温度为109℃。
6.根据权利要求1所述的超高CO2含量合成气脱碳方法,其特征在于:所述胺再生塔上设置有液位报警器,用以方便补充胺再生塔内的胺溶液量。
7.根据权利要求1所述的超高CO2含量合成气脱碳方法,其特征在于:所述胺再生塔上设置有压力调节阀,用以控制胺再生塔顶部压力。
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