Process for Producing Ammonia Synthesis Gas and a Method for Revamping a Front-End of an Ammonia Plant

Abstract

A process for producing ammonia make-up synthesis gas and a procedure for revamping a front-end of an ammonia plant for producing ammonia make-up synthesis gas are disclosed, wherein the make-up synthesis gas is produced by means of steam reforming of a hydrocarbon gaseous feedstock; said front-end includes a primary reformer, a secondary reformer, a shift conversion section, a CO2 removal section and optionally a methanation section; a shell-and-tube gas-heated reformer is installed after said secondary reformer, and a portion of the available feedstock is reformed in the tubes of said gas-heated reformer, and heat is provided to the shell side of said gas-heated reformer by at least a portion of product gas leaving the secondary reformer, possibly mixed with product gas leaving the tubes of said gas-heated reformer.

1 . A procedure for revamping a front-end of an ammonia plant, said front-end being arranged to produce ammonia synthesis gas containing hydrogen and nitrogen by steam reforming of a hydrocarbon gaseous feedstock, said front-end including a primary reformer, a secondary reformer or an autothermal reformer, a shift conversion section, a CO2 removal section and optionally a methanation section, said procedure including at least:
 installation of a gas-heated reformer after said secondary reformer, said gas-heated reformer being a shell-and-tube heat exchanger having a tube side and a shell side, and providing a catalytic reforming of a first gas current passing in the tube side and indirect heating of said first gas current by a second current traversing the shell side,   said first current including a portion of the available hydrocarbon feedstock, the remaining portion of said feedstock being directed to said primary reformer, and said second current comprising at least a portion of a product gas effluent from said secondary reformer or autothermal reformer.   
     
     
         2 . The procedure of  claim 1 , wherein said first current is a portion of a mixed flow comprising steam and the available hydrocarbon feedstock, which is redirected to said gas-heated reactor while the remaining portion is directed to said primary reformer. 
     
     
         3 . The procedure of  claim 2 , said mixed flow having a steam-to-carbon ratio of between 2 and 3.5. 
     
     
         4 . The procedure of  claim 1 , said second current comprising product gas effluent from said secondary reformer or autothermal reformer, and also comprising product gas leaving said tube side of said gas-heated reformer. 
     
     
         5 . The procedure of  claim 1 , said secondary reformer being an air-fired secondary reformer, and the procedure including the step of modifying said secondary reformer to operate with O2-enriched air. 
     
     
         6 . The procedure of  claim 5 , said O2-enriched air being obtained by adding an oxygen flow to ambient air. 
     
     
         7 . The procedure of  claim 6 , said oxygen flow being in an amount to provide a molar concentration of oxygen in the enriched air between 25% and 70%. 
     
     
         8 . The procedure of  claim 6 , said oxygen flow being delivered by an air-separation unit. 
     
     
         9 . The procedure of  claim 8 , further comprising the provision and the installation of said air-separation unit. 
     
     
         10 . The procedure of  claim 1 , further including the revamping of said shift conversion section and/or the revamping of said CO2 removal section. 
     
     
         11 . The procedure of  claim 10 , including the revamping of said shift conversion section by means of one or more of the following: the conversion of one or more existing axial-flow shift converters into axial-radial shift converters; adding one or more shift converters in parallel to the existing ones; replacing one or more existing adiabatic high-temperature shift converters with one or more isothermal medium-temperature shift converters. 
     
     
         12 . The procedure of  claim 11 , including the provision of one or more isothermal medium-temperature shift converters or the modification of one or more existing shift converters to operate as medium shift converters, wherein said medium-temperature shift converters include a copper-based catalyst, and comprise a heat exchanger immersed in the catalyst, to remove the heat produced by the exothermic shift conversion. 
     
     
         13 . The procedure of  claim 12 , said medium temperature being in the range of 200-300° C. 
     
     
         14 . The procedure of  claim 1 , comprising the installation of a purification section after said CO2 removal section, for removal of inert gas from CO2-depleted product gas effluent form said CO2 removal section. 
     
     
         15 . The procedure of  claim 14 , said purification section including a methanation section. 
     
     
         16 . The procedure of  claim 14 , said purification section including a nitrogen wash section or a cryogenic condensation section for condensation of nitrogen and inerts, or a PSA unit. 
     
     
         17 . The procedure of  claim 16 , said purification section including a nitrogen wash section or a cryogenic condensation section, said procedure including the provision of a nitrogen line for addition of nitrogen before or into said nitrogen wash section or said cryogenic condensation section, and said nitrogen being in an amount suitable to obtain a purified synthesis gas containing hydrogen and nitrogen in a molar ratio around 3 to 1. 
     
     
         18 . A process for producing ammonia synthesis gas containing hydrogen and nitrogen by steam reforming of a hydrocarbon gaseous feedstock, including:
 mixing said hydrocarbon gaseous feedstock with steam,   reforming a first portion of the so obtained mixed flow of gaseous feedstock and steam in a primary reformer and then in a secondary reformer or in an autothermal reformer, obtaining a first product gas,   reforming a second portion of said mixed flow in a gas-heated reactor, obtaining a second product gas,   said gas-heated reactor being heated by a current of product gas comprising at least a portion said first product gas.   
     
     
         19 . The process of  claim 18 , said secondary reformer or autothermal reformer operating with O2-enriched air having a concentration of oxygen between 25% and 70% molar. 
     
     
         20 . The process of  claim 18 , further comprising the treatment of product gas comprising: shift conversion, removal of carbon dioxide, and purification of CO2-depleted product gas after said removal of carbon dioxide, and said purification including at least one of the following: a methanation process; nitrogen wash; cryogenic condensation; pressure-swing adsorption (PSA). 
     
     
         21 . A plant for producing ammonia synthesis gas containing hydrogen and nitrogen by reforming of a mixed flow of a gaseous hydrocarbon gaseous feedstock and steam, said plant including:
 a train including a primary reformer and a secondary reformer or an autothermal reformer,   a gas-heated reactor,   said gas-heated reactor being in parallel to said train of primary reformer and secondary reformer or autothermal reformer,   said gas-heated reactor having a tube side for reforming and a shell side for a gaseous heat source,   said plant comprising feeding lines arranged to feed a first portion of said mixed gaseous feedstock and steam to said primary reformer and then to said secondary reformer or autothermal reformer, and to feed a second portion of said mixed gaseous feedstock and steam to said gas-heated reactor,   and said plant comprising a line feeding at least a portion of product gas from said secondary reformer or autothermal reformer to the shell side of said gas-heated reactor.