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1.发明公开Improved low severity hydrocarbon steam reforming process 失效Verfahren vom“低度严重性”-Typ zur Dampfreformierung von Kohlenwasserstoffen。
公开(公告)号：EP0145288A2
公开(公告)日：1985-06-19
申请号：EP84307757.9
申请日：1984-11-09
CPC分类号： C01C1/0405 , C01B3/025 , Y02P20/52
摘要： 0 In a process for producing ammonia which comprises: primary (4) and secondary (60) catalytically reforming shift conversion (80 and 90); carbon oxides removal (115); and ammonia synthesis (110), wherein at least a portion of an ammonia-depleted gas stream is recycled to the synthesis zone (110); and sidestream (134) of the ammonia-depleted gas is treated to separate a stream (142) enriched in hydrogen for return to the ammonia synthesis zone; the improvement which comprises: (i) operating step (b) at a temperature in the outlet gas of not greater than about 946°C and with an amount of air sufficient to provide from about 3 to 11 molar % excess N 2 and to form a secondary reformer outlet gas containing at least 0.8 vol. % methane; (ii) operating step (e) under conditions sufficient to provide at least 10 vol. % inert gases in the ammonia-depleted gas stream; and (iii) introducing as synthesis gas feed to the ammonia synthesis zone a mixture comprising the synthesis gas formed in step (d) having a methane content of at least about 1.2 mol.% CH 4 , on a dry basis, the recycled gas produced in step (f) plus the hydrogen-enriched gas stream formed in step (g), whereby the H 2 loss from the process with the separated inerts enriched gas stream is minimized.
摘要翻译： 在生产氨的方法中，其包括：初级（4）和二级（60）催化重整移动转换（80和90）; 去除碳氧化物（115）; 和氨合成（110），其中至少部分氨贫的气流被再循环到合成区（110）中; 处理贫氨气体的侧流（134）以分离富含氢的流（142）以返回到氨合成区; 改进包括：（i）在出口气体的温度下操作步骤（b）不大于约946℃，并具有足以提供约3至11摩尔％过量的N 2的空气的量，并形成 二次重整器出口气体含有至少0.8vol。 甲烷％ （ii）在足以提供至少10体积％的条件下操作步骤（e） 贫氨气中的惰性气体％; 和（iii）作为合成气进料导入氨合成区，包含在步骤（d）中形成的合成气的混合物，其中甲烷含量为至少约1.2mol％CH4，其干燥的基础是在 步骤（f）加上在步骤（g）中形成的富氢气流，由此使具有分离的惰性气体富集气流的方法中的H 2损失最小化。
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公开(公告)号：EP0145288A3
公开(公告)日：1988-05-11
申请号：EP84307757
申请日：1984-11-09
CPC分类号： C01C1/0405 , C01B3/025 , Y02P20/52
摘要： 0 In a process for producing ammonia which comprises: primary (4) and secondary (60) catalytically reforming shift conversion (80 and 90); carbon oxides removal (115); and ammonia synthesis (110), wherein at least a portion of an ammonia-depleted gas stream is recycled to the synthesis zone (110); and sidestream (134) of the ammonia-depleted gas is treated to separate a stream (142) enriched in hydrogen for return to the ammonia synthesis zone; the improvement which comprises: (i) operating step (b) at a temperature in the outlet gas of not greater than about 946°C and with an amount of air sufficient to provide from about 3 to 11 molar % excess N 2 and to form a secondary reformer outlet gas containing at least 0.8 vol. % methane; (ii) operating step (e) under conditions sufficient to provide at least 10 vol. % inert gases in the ammonia-depleted gas stream; and (iii) introducing as synthesis gas feed to the ammonia synthesis zone a mixture comprising the synthesis gas formed in step (d) having a methane content of at least about 1.2 mol.% CH 4 , on a dry basis, the recycled gas produced in step (f) plus the hydrogen-enriched gas stream formed in step (g), whereby the H 2 loss from the process with the separated inerts enriched gas stream is minimized.
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公开(公告)号：EP0121355A3
公开(公告)日：1988-06-08
申请号：EP84301484
申请日：1984-03-06
CPC分类号： C01C1/0423 , B01J8/0005 , B01J8/0415 , B01J8/0492 , C01C1/0405 , C01C1/0417 , Y02P20/129 , Y02P20/52
摘要： The present invention is generally directed (Figure 2) to an improved process and apparatus for the production of gaseous products such as ammonia by catalytic, exothermic gaseous reactions and is specifically directed to an improved process which utilizes a gas-phase catalytic reaction of nitrogen and hydrogen for the synthesis of ammonia. This improved process for the production of ammonia utilizes an ammonia converter apparatus 110 designed to comprise at least two catalyst stages 102 and 106 and a reheat exchanger 104 so arranged as to provide indirect heat exchange of the gaseous effluent 107 from the last reactor catalyst stage 106 with the effluent from at least one other reactor catalyst stage (e.g., 103) having a higher temperature level in orderto reheat the effluent from the last reactor catalyst stage 107 prior to exiting the reactorvessel 110, thereby facilitating higher level heat recovery from the reactor effluent.
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公开(公告)号：EP0200825A1
公开(公告)日：1986-11-12
申请号：EP85303250.6
申请日：1985-05-08
CPC分类号： C01B3/382 , C01B3/388 , C01B2203/143 , C01B2203/147 , C01B2203/82 , Y02P20/129
摘要： Referring to Figure 1 the hydrocarbon gas feedstream (6) is partially reformed at elevated temperatures in indirect heat exchange with hot combustion gases in a direct fired primary reforming furnace (10) provided with a convection section (4) for recovery of combustion gas treat; and (b) the partially reformed feedstream (58) is then further reformed in the presence of an oxygen-containing gas and stream in a secondary reformer (60) to form a secondary reformer gaseous effluent (62); the improvement which comprises heating a high pressure saturated steam (82) in a first steam superheating zone (80) by indirect heat exchange with at least a portion of said secondary reformer effluent gas (76) to form a first superheated steam stream (84); and (ii) further heating said first superheated steam in a second steam superheating zone (25) by indirect heat exchange with at least a portion of said primary reformer hot combustion gases to form a second superheated steam stream (36).
摘要翻译： 参照图1的烃类气体进料流（6）在与在直接燃烧初级重整炉设置有用于燃烧气体的治疗的回收的对流部分（4）的热燃烧气体（10）进行间接热交换升高的温度下被部分重整; 和（b）所述部分重整的进料流（58）然后进一步在含氧气体和流在次级重整（60）的存在下重整以形成次级重整气体流出物（62）; 该方法包括在由与至少所述的次级重整器流出物的气体（76）的一部分进行间接热交换的第一蒸汽过热区（80）加热的高压饱和蒸汽（82）的改进，以形成第一过热蒸汽流（84） ; 和（ii）进一步加热所述第一过热蒸汽通过与所述初级重整器的热燃烧气体的至少一部分的间接热交换的第二蒸汽过热区域（25），以形成第二过热蒸汽流（36）。
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公开(公告)号：EP0121355B1
公开(公告)日：1991-09-11
申请号：EP84301484.6
申请日：1984-03-06
CPC分类号： C01C1/0423 , B01J8/0005 , B01J8/0415 , B01J8/0492 , C01C1/0405 , C01C1/0417 , Y02P20/129 , Y02P20/52
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公开(公告)号：EP0145211A1
公开(公告)日：1985-06-19
申请号：EP84307416.2
申请日：1984-10-26
IPC分类号： C01B3/38
CPC分类号： C01B3/382 , C01B2203/143 , C01B2203/147 , C01B2203/82 , Y02P20/129
摘要： Referring to Figure 1 the hydrocarbon gas feedstream (6) is partially reformed at elevated temperatures in indirect heat exchange with hot combustion gases in a direct fired primary reforming furnace (10) provided with a convection section 14) for recovery of combustion gas treat: and (b) the partially reformed feedstream (58) is then further reformed in the presence of an oxygen-containing gas and steam in a secondary reformer (60) to form a secondary reformer gaseous effluent (62); the improvement which comprises heating a high pressure saturated steam (82) in a first steam superheating zone (80) by indirect heat exchange with at least a portion of said secondary reformer effluent gas (76) to form a first superheated steam stream (84); and (ii) further heating said first superheated steam in a second steam superheating zone (25) by indirect heat exchange with at least a portion of said primary reformer hot combustion gases to form a second superheated steam stream (36).
摘要翻译： 参照图1的烃类气体进料流（6）在与在直接燃烧初级重整炉设置有用于燃烧气体的治疗的回收的对流部分（4）的热燃烧气体（10）进行间接热交换升高的温度下被部分重整; 和（b）所述部分重整的进料流（58）然后进一步在含氧气体和蒸汽的在二段转化炉（60）的存在下重整以形成次级重整气体流出物（62）; 该方法包括在由与至少所述的次级重整器流出物的气体（76）的一部分进行间接热交换的第一蒸汽过热区（80）加热的高压饱和蒸汽（82）的改进，以形成第一过热蒸汽流（84） ; 和（ii）进一步加热所述第一过热蒸汽通过与所述初级重整器的热燃烧气体的至少一部分的间接热交换的第二蒸汽过热区域（25），以形成第二过热蒸汽流（36）。
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公开(公告)号：EP0121355A2
公开(公告)日：1984-10-10
申请号：EP84301484.6
申请日：1984-03-06
CPC分类号： C01C1/0423 , B01J8/0005 , B01J8/0415 , B01J8/0492 , C01C1/0405 , C01C1/0417 , Y02P20/129 , Y02P20/52
摘要： The present invention is generally directed (Figure 2) to an improved process and apparatus for the production of gaseous products such as ammonia by catalytic, exothermic gaseous reactions and is specifically directed to an improved process which utilizes a gas-phase catalytic reaction of nitrogen and hydrogen for the synthesis of ammonia. This improved process for the production of ammonia utilizes an ammonia converter apparatus 110 designed to comprise at least two catalyst stages 102 and 106 and a reheat exchanger 104 so arranged as to provide indirect heat exchange of the gaseous effluent 107 from the last reactor catalyst stage 106 with the effluent from at least one other reactor catalyst stage (e.g., 103) having a higher temperature level in orderto reheat the effluent from the last reactor catalyst stage 107 prior to exiting the reactorvessel 110, thereby facilitating higher level heat recovery from the reactor effluent.
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