CN109099642A - 一种洁净煤气生产lng联产氮氢气、富co的方法及装置 - Google Patents

一种洁净煤气生产lng联产氮氢气、富co的方法及装置 Download PDF

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CN109099642A
CN109099642A CN201811081014.5A CN201811081014A CN109099642A CN 109099642 A CN109099642 A CN 109099642A CN 201811081014 A CN201811081014 A CN 201811081014A CN 109099642 A CN109099642 A CN 109099642A
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gas
heat exchanger
rectifying column
nitrogen
exchanger group
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虎骁
王蕾
相里国栋
杨波
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Shaanxi Black Cat Coking Co Ltd
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Shaanxi Black Cat Coking Co Ltd
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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Abstract

本发明公开了一种洁净煤气生产LNG联产氮氢气、富CO的方法及装置，由以下步骤组成：以洁净煤气为基础，进行干燥，得到第一处理气；除去汞，得到第二处理气；除去二氧化碳、重烃和粉尘，得到第三处理气；对第三处理气降温后经重烃分离器得到LPG和气液混合物，对气液混合物继续降温后经过脱氢处理得到富氢气气体和第一处理液；采用液体氮气在洗涤塔中对富氢气气体中的甲烷和CO进行脱除；对第一处理液脱碳处理得到富CO气体和LNG；本发明解决了冷箱通道发生重烃冻堵的问题，冷箱内设置洗涤塔，脱除富氢气中的CO和甲烷。

Description

一种洁净煤气生产LNG联产氮氢气、富CO的方法及装置
【技术领域】
本发明属于焦炉煤气净化处理、液化分离技术领域，尤其涉及一种洁净煤气生产LNG联产氮氢气、富CO的方法及装置。
【背景技术】
焦炉煤气，又称焦炉气，可燃成分多，属于高热值煤气，粗煤气或荒煤气。是炼焦用煤在炼焦炉中经过高温干馏后，产出焦炭和焦油产品的同时所产生的一种可燃性气体，是炼焦工业的副产品。其主要成分为氢气(55％～60％)和甲烷(23％～27％)，另外还含有少量的一氧化碳(5％～8％)、C2以上不饱和烃(2％～4％)、二氧化碳(1.5％～3％)、氧气(0.3％～0.8％))、氮气(3％～7％)及硫化物等。其中氢气、甲烷、一氧化碳、C2以上不饱和烃为可燃组分，二氧化碳、氮气、氧气为不可燃组分。
目前焦炉煤气一部分用来发电，一部分用来生产甲醇和制氢，还有相当一部分直接燃烧和排放，其能量利用率约为55％，在浪费宝贵资源的同时，也对环境造成了极大的污染，所以，对焦炉煤气的处理受到人们的关注。
同时，LNG(液化天然气)是一种清洁、高效的能源。由于进口LNG有助于能源消费国实现能源供应多元化、保障能源安全，而出口LNG有助于天然气生产国有效开发天然气资源、增加外汇收入、促进国民经济发展，因而LNG贸易正成为全球能源市场的新热点。
目前焦炉煤气的应用主要为利用氢气制甲醇或合成氨，或利用甲烷化增产甲烷制LNG，两种方式要么对甲烷的经济价值利用率不高，要么对氢气的利用价值不高，合成氨的常规的生产方法是净化后的焦炉煤气制取LNG，富氢气在冷箱外与氮气混合到一定比例生产合成氨，因此本工艺同时产氢气、CO和LNG，实现焦炉煤气经济价值最大化利用。
【发明内容】
本发明的目的是提供一种洁净煤气生产LNG联产氮氢气、富CO的方法及装置，以解决洁净煤气生产LNG过程前，需进行过膜脱水处理；生产LNG过程中重烃造成冷箱冻堵；产出的送往合成氨的富氢气气体中氮气含量少的问题。
本发明采用以下技术方案：一种洁净煤气生产LNG联产氮氢气、富CO的方法，由以下步骤组成：
a.以洁净煤气为基础，对洁净煤气进行干燥，除去水分，得到第一处理气；
b.除去第一处理气中汞，得到第二处理气；
c.除去第二处理气中的二氧化碳、重烃和粉尘，得到第三处理气；
d.对第三处理气降温后经重烃分离器得到LPG和气液混合物；
e.对气液混合物继续降温后经过脱氢处理得到富氢气气体和第一处理液；
f.采用液体氮气在洗涤塔中对富氢气气体中的甲烷和CO进行脱除，得到甲烷和CO含量低于1ppm的氮氢气气体；对第一处理液脱碳处理得到富CO气体和LNG。
进一步地，步骤d和e的降温步骤采用双冷源双通道的换热器组，换热器组包括依次串联的一级换热器组、二级换热器组和三级换热器组，一级换热器组、二级换热器组和三级换热器组的换热器的个数分别为8个、8个和4个。
进一步地，双冷源为液相冷源和气相冷源。
进一步地，液相冷源由氮气、甲烷、乙烯、丙烷和异戊烷组成。
进一步地，液相冷源的氮气含量为10-15％、甲烷含量为35-45％、乙烯含量为20-25％、丙烷含量为8-15％、异戊烷的含量为10-20％。
进一步地，液相冷源的氮气含量为12.3％、甲烷含量为40.9％、乙烯含量为18.4％、丙烷含量为12.6％、异戊烷的含量为15.8％。
进一步地，换热器组的液相冷源和气相冷源的通道分开设置。
一种的洁净煤气生产LNG联产富氢气、富CO的装置，包括依次连接的干燥单元、吸附单元、纯化单元和分离单元；
干燥单元包括干燥塔，吸附单元包括吸附塔，纯化单元包括依次串联的纯化塔和粉尘过滤器，分离单元位于冷箱内，分离单元包括换热器组、重烃分离器、脱氢精馏塔、洗涤塔和脱碳精馏塔；
干燥塔用于以洁净煤气为基础，对洁净煤气进行干燥，除去水分，得到第一处理气，干燥塔通过管道连接至吸附塔，吸附塔用于第一处理气从其底部进入自下而上经活性炭脱除汞，得到第二处理气，吸附塔通过管道连接至纯化塔，纯化塔用于第二处理气从其底部进入自下而上经床层吸附剂脱除二氧化碳和重烃，纯化塔通过管道连接至粉尘过滤器，粉尘过滤器用于过滤第二处理气中的粉尘，得到第三处理气，粉尘过滤器通过换热器组连接至重烃分离器，重烃分离器用于将第三处理气进行分离后得到气液混合物和LPG；
重烃分离器通过二级换热器组和三级换热器组连接至脱氢精馏塔，脱氢精馏塔用于将气液混合物分离成富氢气气体和第一处理液，脱氢精馏塔的顶部和底部分别通过管道连接至洗涤塔和脱碳精馏塔，脱氢精馏塔的顶部管道用于富氢气气体流入洗涤塔，脱氢精馏塔的底部管道用于第一处理液流入脱碳精馏塔，洗涤塔用于液体氮气从顶部进入脱除富氢气气体中的甲烷和CO，洗涤塔的底部通过三级换热器组还连接至脱碳精馏塔，脱碳精馏塔用于将第一处理液以及流入脱碳精馏塔底部的剩余液体分离成富CO气体和LNG。
进一步地，脱氢精馏塔的顶部通过分离器连接至洗涤塔，分离器用于对富氢气进行气液分离。
进一步地，分离器底部通过管道连接有过冷器，过冷器用于对富氢气气体进一步冷却，过冷器通过三级换热器组连接至所述脱碳精馏塔。
本发明的有益效果是：1、设置纯化单元和冷箱内LPG低温采出，解决了冷箱通道发生重烃冻堵的问题，采出的LPG送往LPG罐区作为副产品卖出，增加了产品附加值。2、混合制冷工艺采用采用双冷源的换热器，并进行低温分离节流，使温场温度调节反馈更灵敏，系统能耗大大降低。3、冷箱内设置洗涤塔，依据低温液氮洗原理，通过低温液氮与富氢气对流将CO和甲烷脱除，塔顶产出的富氢气中的氮气含量高，只需配入少量氮气即可达到氮氢比3:1后用于合成氨生产，与富氢气冷箱外配氮相比，能耗降低。4.通过设置辅助干燥塔避免洁净煤气生产LNG过程前，进行过膜脱水处理，减少了能耗，降低了生产成本。
【附图说明】
图1为本发明的结构示意图。
其中：1.干燥塔；2.吸附塔；3.纯化塔；4.粉尘过滤器；5.重烃分离器；6.脱氢精馏塔；7.过冷器；8.洗涤塔；9.脱碳精馏塔；10.三级换热器组；11.分离器；12.一级换热器组；13.二级换热器组。
【具体实施方式】
下面结合附图和具体实施方式对本发明进行详细说明。
本发明公开了一种洁净煤气生产LNG联产氮氢气、富CO的方法，由以下步骤组成：
a.以洁净煤气为基础，对洁净煤气进行干燥，除去水分，得到第一处理气；
b.除去第一处理气中汞，得到第二处理气；
c.除去第二处理气中的二氧化碳、重烃和粉尘，得到第三处理气；第三处理气的露点温度＜-65摄氏度，CO2含量＜50ppm，汞＜0.01μg/m3，重烃含量减少；
d.对第三处理气经一级换热器组12降温后经重烃分离器5得到LPG和气液混合物，净化合格的煤气进入冷箱，经过一级换热器组12，冷箱内LPG低温采出，解决了冷箱通道发生重烃冻堵的问题，采出的LPG送往LPG罐区作为副产品卖出，增加了产品附加值，此时原料气中的绝大部分甲烷以及部分一氧化碳和少量氮气变成液体得到气液混合物；
e.对气液混合物降温后经过脱氢处理得到富氢气气体和第一处理液；气液混合物经过脱氢精馏塔6分离后得到富氢气气体和第一处理液，富氢气气体即以氢气为主的气态流体从脱氢精馏塔6顶部出来，进入分离器11进行气液分离处理，分离出的气体进入洗涤塔8，分离出的液体经过过冷器7和三级换热器组10降温后进入脱碳精馏塔9；
f.采用液体氮气在洗涤塔8中对富氢气气体中的甲烷和CO进行脱除，得到甲烷和CO含量低于1ppm的氮氢气气体，经过液氮洗涤以后将富氢气气体中的CO和甲烷脱出，然后富氢气气体从洗涤塔8依次返回换热器组复热，最后出冷箱，送往化肥厂作为生产合成氨的原料。
对第一处理液以及分离器11分离后的液体脱碳处理得到富CO气体和LNG，第一处理液直接进入脱碳精馏塔9，分离器11分离后的液体经过过冷器7和三级换热器组10降温后进入脱碳精馏塔9，通过热质交换，不断被提浓至LNG纯度高于90％后从脱碳精馏塔9塔底采出，最后经过冷却，成为过冷LNG产品送往LNG储槽，在LNG储槽顶部节流产生常压低温的液体产品。
脱碳精馏塔9顶部出来的尾气以一氧化碳为主，同时有氮气、氢气及微量甲烷简称富一氧化碳气，依次返回换热器组复热，最后送出冷箱，得到富一氧化碳气产品。
步骤d和e的降温步骤采用双冷源双通道的换热器组，并进行低温分离节流，使温场温度调节反馈更灵敏，系统能耗大大降低，换热器为板翅式换热器，换热器组包括依次串联的一级换热器组12、二级换热器组13和三级换热器组10，一级换热器组12、二级换热器组13和三级换热器组10的换热器的个数分别为8个、8个和4个，双冷源为液相冷源和气相冷源，液相冷源和气相冷源由氮气、甲烷、乙烯、丙烷和异戊烷组成，液相冷源的氮气含量为10-15％、甲烷含量为35-45％、乙烯含量为20-25％、丙烷含量为8-15％、异戊烷的含量为10-20％，作为优选的液相冷源的氮气含量为12.3％、甲烷含量为40.9％、乙烯含量为18.4％、丙烷含量为12.6％、异戊烷的含量为15.8％，虽然液相冷源和气相冷源的组成成分一致，但是两个通道内的冷源的状态不一致，液相冷源通道内的冷源为液相，气相冷源通道内的冷源为气相，而且两个通道的状态会随着温度的变化逐渐发生变化。
液相冷源进入主换热器，降温至-55℃，经过节流阀节流后，为换热器提供冷量；气相冷源进入冷箱，依次经一级换热器组12、二级换热器组13降温后，送至脱碳精馏塔9塔底提供再沸热量，再经三级换热器组10降温至-160℃，经过节流阀节流后，依次返回主换热器为其提供冷量，充分复温后出界区。
脱氢精馏塔6顶部、脱碳精馏塔9顶部的冷凝器需要温度非常低，因此采用氮气为其提供必要的低温冷量，氮气进入冷箱，经三级换热器组10及过冷器7换热后，温度降至-180℃，分别经过节流后，分别为脱氢精馏塔6顶部、脱碳精馏塔9顶部的冷凝器提供冷量，而后依次通过过冷器7、主换热器、充分复温后出冷箱。
本发明还公开了一种洁净煤气生产LNG联产氮氢气、富CO的装置，如图1所示，包括依次连接的干燥单元、吸附单元、纯化单元和分离单元；
干燥单元：
干燥单元包括干燥塔1，干燥单元的干燥塔1用于以洁净煤气为基础，对洁净煤气进行干燥，除去水分，得到第一处理气；干燥塔1通过管道连接至吸附塔2，干燥单元由2台干燥塔1、1台辅助干燥塔1、1台加热器、1台冷却器、1台分离器11及1台冷凝液罐组成。当一台干燥塔1在吸附的过程中，另外一台干燥塔1和辅助干燥塔1在进行加热和冷却，两台干燥塔1轮流操作，每台干燥塔1的吸附周期为8小时，整个干燥过程的实施由程控阀自动切换实现连续操作，干燥后的产品气体露点低于-70℃。
吸附单元：
吸附单元包括吸附塔2，吸附单元的吸附塔2通过管道连接至干燥塔1，吸附塔2用于第一处理气从其底部进入自下而上经活性炭脱除汞，得到第二处理气，吸附塔2通过管道连接至纯化塔3；来自于干燥工序的第一处理气，温度为40℃、流量127000Nm3/h，从底部进入吸附塔2自下而上经活性炭脱除第一处理气中的汞，继而进入纯化工序。
纯化单元：
纯化单元依次串联有纯化塔3和粉尘过滤器4，纯化塔3通过管道连接至吸附塔2，纯化塔3用于第二处理气从其底部进入自下而上经床层吸附剂脱除二氧化碳和重烃，纯化塔3通过管道连接至粉尘过滤器4，粉尘过滤器4用于过滤第二处理气中的粉尘，得到第三处理气，粉尘过滤器4通过换热器组连接至重烃分离器5；经过吸附工序后的第二处理气进入纯化工序。纯化单元采用“分子筛+活性炭”三塔纯化工艺，利用符合床层吸附剂在不同压力和温度下吸附容量存在差异和选择吸附的特性，脱除原料气中的二氧化碳、重烃以满足液化分离单元的要求。
纯化单元由3台纯化塔3、1台加热器、1台冷却器、1台分离器11及1台冷凝液罐组成。当一台纯化塔3在吸附的过程中，另外两台纯化塔3在进行加热和冷却，三台纯化塔3轮流操作，每台纯化塔3的吸附周期为8小时，整个干燥过程的实施有程控阀的自动切换实现连续操作，干燥后的产品气体露点低于-70℃。
分离单元：
分离单元位于冷箱内，分离单元包括换热器组、重烃分离器5、脱氢精馏塔6、洗涤塔8和脱碳精馏塔9，重烃分离器5通过一级换热器组12连接至粉尘过滤器4，重烃分离器5用于将第三处理气进行分离后得到气液混合物和LPG，重烃分离器5还通过二级换热器组13和三级换热器组10连接至脱氢精馏塔6，脱氢精馏塔6用于将气液混合物分离成富氢气气体和第一处理液，脱氢精馏塔6的顶部和底部分别通过管道连接至洗涤塔8和脱碳精馏塔9，脱氢精馏塔6的顶部管道用于富氢气气体进入洗涤塔8，脱氢精馏塔6的底部管道用于第一处理液流入脱碳精馏塔9，洗涤塔8用于液体氮气从顶部进入脱除富氢气气体中的甲烷和CO，脱碳精馏塔9用于将第一处理液以及进入脱碳精馏塔9底部的剩余液体分离成富CO气体和LNG。
第三处理气进入冷箱，经过一级换热器组12降温至-55℃，进入重烃分离器5，得到LPG和气液混合物，重烃分离器5底部采出LPG送出冷箱，气液混合物进入二级换热器组13继续降温，经换热器组降温后进入脱氢精馏塔6。
脱氢精馏塔6的顶部通过分离器11连接至洗涤塔8，分离器11用于对富氢气进行气液分离，富氢气气体即以氢气为主的气态流体从脱氢精馏塔6顶部出来，进入分离器11进行气液分离处理，分离出的气体进入洗涤塔8，洗涤塔8的底部通过三级换热器组10还连接至脱碳精馏塔9，分离出的液体经过过冷器7和三级换热器组10降温后进入脱碳精馏塔9，分离器11底部通过管道连接有过冷器7，过冷器7用于对富氢气气体进一步冷却，过冷器7通过三级换热器组10连接至脱碳精馏塔9，第一处理液直接进入脱碳精馏塔9，分离器11分离后的液体经过过冷器7和三级换热器组10降温后流入脱碳精馏塔9，通过热质交换，不断被提浓至LNG纯度高于90％后从脱碳精馏塔9塔底采出，最后经过冷却，成为过冷LNG产品送往LNG储槽，在LNG储槽顶部节流产生常压低温的液体产品。
中压氮气经换热器组降温后进入洗涤塔8的顶部，在洗涤塔8内来自塔顶的液氮与来自塔底的原料气充分接触，在塔内经热质交换，将富氢气气体中的甲烷和一氧化碳脱除至1ppm以下，然后经换热器组复温后出冷箱，冷箱内设置洗涤塔8，依据低温液氮洗原理，通过低温液氮与富氢气对流将CO和甲烷脱除，塔顶产出的富氢气中的氮气含量高，只需配入少量氮气即可达到氮氢比3:1后用于合成氨生产，与富氢气冷箱外配氮相比，能耗降低。
第一处理液直接流入脱碳精馏塔9，分离器11分离后的液体经过过冷器7和三级换热器组10降温后进入脱碳精馏塔9，在脱碳精馏塔9中，从塔顶排出的富一氧化碳气，经换热器组复温后出界区，脱碳精馏塔9塔底采出的LNG产品经换热器组降温至-162℃后出界区。

Claims (10)

1.一种洁净煤气生产LNG联产氮氢气、富CO的方法，其特征在于，由以下步骤组成：
a.以洁净煤气为基础，对洁净煤气进行干燥，除去水分，得到第一处理气；
b.除去所述第一处理气中汞，得到第二处理气；
c.除去所述第二处理气中的二氧化碳、重烃和粉尘，得到第三处理气；
d.对所述第三处理气降温后经重烃分离器(5)得到LPG和气液混合物；
e.对所述气液混合物降温后经过脱氢处理得到富氢气气体和第一处理液；
f.采用液体氮气在洗涤塔(8)中对所述富氢气气体中的甲烷和CO进行脱除，得到甲烷和CO含量低于1ppm的氮氢气气体；对所述第一处理液脱碳处理得到富CO气体和LNG。
2.根据权利要求1所述的一种洁净煤气生产LNG联产氮氢气、富CO的方法及装置，其特征在于，所述步骤d和e的降温步骤采用双冷源双通道的换热器组，所述换热器组包括依次串联的一级换热器组(12)、二级换热器组(13)和三级换热器组(10)，所述一级换热器组(12)、二级换热器组(13)和三级换热器组(10)的换热器的个数分别为8个、8个和4个。
3.根据权利要求2所述的一种洁净煤气生产LNG联产氮氢气、富CO的方法及装置，其特征在于，所述双冷源为液相冷源和气相冷源。
4.根据权利要求3所述的一种洁净煤气生产LNG联产氮氢气、富CO的方法及装置，其特征在于，所述液相冷源和气相冷源由氮气、甲烷、乙烯、丙烷和异戊烷组成。
5.根据权利要求4所述的一种洁净煤气生产LNG联产氮氢气、富CO的方法及装置，其特征在于，所述液相冷源和气相冷源的氮气含量为10-15％、甲烷含量为35-45％、乙烯含量为20-25％、丙烷含量为8-15％、异戊烷的含量为10-20％。
6.根据权利要求4所述的一种洁净煤气生产LNG联产氮氢气、富CO的方法及装置，其特征在于，所述液相冷源和气相冷源的氮气含量为12.3％、甲烷含量为40.9％、乙烯含量为18.4％、丙烷含量为12.6％、异戊烷的含量为15.8％。
7.根据权利要求2-6任一所述的一种洁净煤气生产LNG联产氮氢气、富CO的方法及装置，其特征在于，所述换热器组的所述液相冷源和气相冷源的通道分开设置。
8.一种洁净煤气生产LNG联产富氢气、富CO的装置，其特征在于，包括依次连接的干燥单元、吸附单元、纯化单元和分离单元；
所述干燥单元包括干燥塔(1)，所述吸附单元包括吸附塔(2)，所述纯化单元包括依次串联的纯化塔(3)和粉尘过滤器(4)，所述分离单元位于冷箱内，所述分离单元包括换热器组、重烃分离器(5)、脱氢精馏塔(6)、洗涤塔(8)和脱碳精馏塔(9)；
所述干燥塔(1)用于以洁净煤气为基础，对洁净煤气进行干燥，除去水分，得到第一处理气，所述干燥塔(1)通过管道连接至所述吸附塔(2)，所述吸附塔(2)用于所述第一处理气从其底部进入自下而上经活性炭脱除汞，得到第二处理气，所述吸附塔(2)通过管道连接至所述纯化塔(3)，所述纯化塔(3)用于所述第二处理气从其底部进入自下而上经床层吸附剂脱除二氧化碳和重烃，所述纯化塔(3)通过管道连接至所述粉尘过滤器(4)，所述粉尘过滤器(4)用于过滤所述第二处理气中的粉尘，得到第三处理气，所述粉尘过滤器(4)通过换热器组连接至所述重烃分离器(5)，所述重烃分离器(5)用于将所述第三处理气进行分离后得到气液混合物和LPG；
所述重烃分离器(5)通过所述二级换热器组(13)和所述三级换热器组(10)连接至所述脱氢精馏塔(6)，所述脱氢精馏塔(6)用于将所述气液混合物分离成富氢气气体和第一处理液，所述脱氢精馏塔(6)的顶部和底部分别通过管道连接至所述洗涤塔(8)和所述脱碳精馏塔(9)，所述脱氢精馏塔(6)的顶部管道用于所述富氢气气体流入所述洗涤塔(8)，所述脱氢精馏塔(6)的底部管道用于所述第一处理液流入所述脱碳精馏塔(9)，所述洗涤塔(8)用于液体氮气从顶部进入脱除所述富氢气气体中的甲烷和CO，所述洗涤塔(8)的底部通过所述三级换热器组(10)还连接至所述脱碳精馏塔(9)，所述脱碳精馏塔(9)用于将所述第一处理液以及流入所述脱碳精馏塔(9)底部的剩余液体分离成富CO气体和LNG。
9.根据权利要求8所述的一种洁净煤气生产LNG联产富氢气、富CO的装置，其特征在于，所述脱氢精馏塔(6)的顶部通过分离器(11)连接至所述洗涤塔(8)，所述分离器(11)用于对富氢气进行气液分离。
10.根据权利要求8所述的一种洁净煤气生产LNG联产富氢气、富CO的装置，其特征在于，所述分离器(11)底部通过管道连接有过冷器(7)，所述过冷器(7)用于对富氢气气体进一步冷却，所述过冷器(7)通过所述三级换热器组(10)连接至所述脱碳精馏塔(9)。
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114276846A (zh) * 2021-12-16 2022-04-05 陕西黑猫焦化股份有限公司 一种利用焦炉煤气制备lng联产合成氨的方法及系统

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103033025A (zh) * 2011-09-30 2013-04-10 新地能源工程技术有限公司 从富甲烷气中脱氢气、氮气、一氧化碳并生产液化天然气的工艺
WO2015140460A2 (fr) * 2014-03-17 2015-09-24 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de séparation cryogénique d'un gaz de synthèse contenant du monoxyde de carbone, du méthane et de l'hydrogène
CN105258452A (zh) * 2015-10-29 2016-01-20 中国科学院理化技术研究所 热解煤气的气体分离装置及气体分离方法
CN105910387A (zh) * 2016-05-16 2016-08-31 中国石油集团工程设计有限责任公司 一种从焦炉煤气制lng中回收冷量的工艺装置及方法
CN106568298A (zh) * 2016-10-27 2017-04-19 杭州中泰深冷技术股份有限公司 一种焦炉气制lng联产合成氨装置及控制方法
CN107367127A (zh) * 2017-08-15 2017-11-21 成都深冷液化设备股份有限公司 一种深冷分离co、h2的氮循环甲烷洗涤系统及方法
CN208952531U (zh) * 2018-09-17 2019-06-07 陕西黑猫焦化股份有限公司 一种洁净煤气生产lng联产氮氢气、富co的装置

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103033025A (zh) * 2011-09-30 2013-04-10 新地能源工程技术有限公司 从富甲烷气中脱氢气、氮气、一氧化碳并生产液化天然气的工艺
WO2015140460A2 (fr) * 2014-03-17 2015-09-24 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de séparation cryogénique d'un gaz de synthèse contenant du monoxyde de carbone, du méthane et de l'hydrogène
CN105258452A (zh) * 2015-10-29 2016-01-20 中国科学院理化技术研究所 热解煤气的气体分离装置及气体分离方法
CN105910387A (zh) * 2016-05-16 2016-08-31 中国石油集团工程设计有限责任公司 一种从焦炉煤气制lng中回收冷量的工艺装置及方法
CN106568298A (zh) * 2016-10-27 2017-04-19 杭州中泰深冷技术股份有限公司 一种焦炉气制lng联产合成氨装置及控制方法
CN107367127A (zh) * 2017-08-15 2017-11-21 成都深冷液化设备股份有限公司 一种深冷分离co、h2的氮循环甲烷洗涤系统及方法
CN208952531U (zh) * 2018-09-17 2019-06-07 陕西黑猫焦化股份有限公司 一种洁净煤气生产lng联产氮氢气、富co的装置

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114276846A (zh) * 2021-12-16 2022-04-05 陕西黑猫焦化股份有限公司 一种利用焦炉煤气制备lng联产合成氨的方法及系统
CN114276846B (zh) * 2021-12-16 2023-11-07 陕西黑猫焦化股份有限公司 一种利用焦炉煤气制备lng联产合成氨的方法及系统

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