System and method for cryogenic purification of a feed stream comprising hydrogen, methane, nitrogen and argon

A system and method for cryogenic purification of a hydrogen, nitrogen, methane and argon containing feed stream to produce a methane free, hydrogen and nitrogen containing synthesis gas and a methane rich fuel gas, as well as to recover an argon product stream, excess hydrogen, and excess nitrogen is provided. The disclosed system and method are particularly useful as an integrated cryogenic purifier in an ammonia synthesis process in an ammonia plant. The excess nitrogen is a nitrogen stream substantially free of methane and hydrogen that can be used in other parts of the plant, recovered as a gaseous nitrogen product and/or liquefied to produce a liquid nitrogen product.

TECHNICAL FIELD

The present invention relates to an integrated cryogenic purification system and method for chemical plants, such as an ammonia plant. More particularly the present invention relates to a system and method for cryogenic purification and recovery of argon, hydrogen, and nitrogen from a crude synthesis gas feed stream comprising hydrogen, nitrogen, methane and argon to recover argon, as well as excess hydrogen and nitrogen.

BACKGROUND

The availability of low cost natural gas has led to the restart and construction of numerous ammonia production facilities throughout North America. Ammonia is typically produced through steam methane reforming. In the steam methane reforming process, air is used to auto-fire the reaction and to supply nitrogen for the ammonia synthesis reaction. In general, the steam methane reforming based process consists of primary steam reforming, secondary ‘auto-thermal’ steam reforming followed by a water-gas shift reaction and carbon oxide removal processes to produce a synthesis gas. The synthesis gas is subsequently dried to produce a raw nitrogen-hydrogen process gas with small amounts of methane and inerts which is then fed to an ammonia synthesis reaction. In many ammonia production plants, the raw nitrogen-hydrogen process gas is often subjected to a number of purification or additional process steps prior to the ammonia synthesis reaction.

A commercially important part of the ammonia processing train often used in ammonia plants is a cryogenic purification process known by those skilled in the art as the ‘Braun Purifier’. Since the secondary reformer is fed with an air flow having a nitrogen content that is larger than that required by the stoichiometry of the ammonia synthesis reaction, excess nitrogen, unconverted methane and inert gases must be removed or rejected from the raw nitrogen-hydrogen process gas prior to the ammonia synthesis step. In order to reject the excess nitrogen, unconverted methane and inerts, the Braun-type cryogenic purification process is introduced after the methanation reaction. The primary purpose of this Braun-type cryogenic purification process is to generate an overhead ammonia synthesis gas stream with a stoichiometric ratio of hydrogen to nitrogen (H2:N2) of about 3:1 and low levels of methane and inerts.

The cryogenic purification step of the Braun Purifier typically employs a single stage of refrigerated rectification. The overhead synthesis gas stream from the single stage of refrigerated rectification is substantially free of unconverted methane and a substantial portion of the inerts, such as argon, are rejected into the fuel gas stream-bottoms liquid. In the Braun Purifier process, the feed gas stream is first cooled and dehydrated. The feed gas stream is then partially cooled and expanded to a lower pressure. The feed gas stream may be further cooled to near saturation and partially condensed and then directed to the base of the single stage rectifier. The rectifier overhead is the resulting ammonia synthesis gas that is processed for ammonia synthesis, whereas the rectifier bottoms are partially vaporized by passage through the rectifier condenser and warmed to ambient temperatures. This fuel/waste stream is typically directed back to the reformer and serves as fuel. See Bhakta, M., Grotz, B., Gosnell, J., Madhavan, S., “Techniques for Increase Capacity and Efficiency of Ammonia Plants”, Ammonia Technical Manual 1998, which provides additional details of this Braun Purifier process.

The waste gas from the Braun Purifier process step is predominantly a mixture of hydrogen (6.3 mole %), nitrogen (76.3 mole %), methane (15.1 mole %) and argon (2.3 mole %). The conventional argon recovery processes from ammonia tail gas are typically integrated with the hydrogen recovery process downstream of the Braun purifier. The conventional argon recovery processes are relatively complex and involves multiple columns, vaporizers, compressors, and heat exchangers, as described for example in W. H Isalski, “Separation of Gases” (1989) pages 84-88. Other relatively complex argon recovery systems and process are disclosed in U.S. Pat. Nos. 3,442,613; 5,775,128; 6,620,399; 7,090,816; and 8,307,671. Similarly, systems and processes for the recovery of argon, hydrogen and nitrogen from the waste gas are disclosed in U.S. Pat. Nos. 3,666,415; 3,675,434; 4,058,589; 4,077,780; 4,524,056; 4,752,311 and United. States Patent Application Publication No. 2013/0039835; and 2016/0060130. While these waste gas processing solutions adequately recover the argon, hydrogen and nitrogen, they do so at additional capital and operating costs.

What is needed therefore is an efficient and cost effective solution for recovery of the hydrogen, methane, nitrogen, and argon that is preferably integrated with the cryogenic purification of the synthesis gas.

SUMMARY OF THE INVENTION

The present invention may be characterized as a cryogenic purification system configured for purifying a hydrogen, nitrogen, methane and argon containing feed stream, the purification system comprising: (i) a synthesis gas rectification column configured to receive the feed stream and produce a hydrogen and nitrogen enriched overhead vapor stream and a methane-rich condensed phase stream proximate the bottom of the synthesis gas rectification column; (ii) a hydrogen stripping column configured to receive the methane-rich condensed phase stream from the synthesis gas rectification column, strip hydrogen from the methane-rich condensed phase stream and produce a hydrogen free methane bottom stream and a hydrogen enriched gaseous overhead; (iii) a condenser configured to receive the hydrogen free methane bottom stream and a working fluid and to produce a vaporized or partially vaporized hydrogen free methane-rich stream; and (iv) a heat exchanger configured to (a) warm the hydrogen and nitrogen enriched overhead vapor stream via indirect heat exchange with the feed stream to produce a hydrogen and nitrogen containing synthesis gas; and (b) to warm the vaporized or partially vaporized hydrogen free methane-rich stream via indirect heat exchange with the feed stream to produce a methane fuel gas.

The present invention may be characterized as a cryogenic purification system configured for purifying a hydrogen, nitrogen, methane and argon containing feed stream, the cryogenic purification system comprising: (i) a synthesis gas rectification column configured to receive the hydrogen, nitrogen, methane and argon containing feed stream and produce a hydrogen and nitrogen enriched overhead vapor stream and a methane-rich condensed phase stream proximate the bottom of the synthesis gas rectification column; (ii) a condenser-reboiler disposed within the synthesis gas rectification column configured to vaporize the hydrogen free methane bottom stream against a working fluid to produce a vaporized or partially vaporized hydrogen free methane rich stream; (iii) a nitrogen rectification column configured to receive the vaporized or partially vaporized hydrogen free methane bottom stream and a liquid nitrogen reflux stream and produce a nitrogen containing overhead vapor stream substantially free of methane, and a methane enriched liquid bottom stream; (iv) a heat exchanger configured to (a) warm the hydrogen and nitrogen enriched overhead vapor stream via indirect heat exchange with the hydrogen, nitrogen, methane and argon containing feed stream to produce a hydrogen and nitrogen containing synthesis gas; (b) to warm the nitrogen containing overhead vapor stream substantially free of methane to produce a warm gaseous nitrogen stream, and (c) to warm the methane enriched liquid bottom stream to produce a methane fuel gas; and (v) a nitrogen recovery system configured to receive the warm nitrogen containing stream and produce at least one nitrogen product.

In some of the preferred embodiments, the feed gas may be conditioned via pre-purification of the feed stream, further compression or expansion of the feed stream to a pressure that is preferably greater than or equal to about 300 psia, and/or cooling of the feed stream to a temperature near saturation, and warming of the feed stream. The pre-purification of the feed stream may involve removing selected impurities or contaminants from the crude feed stream in an adsorption based pre-purifier or getter.

In embodiments that include hydrogen recovery, the present systems may further include a second heat exchanger configured for cooling the methane-rich condensed phase stream to produce a cooled methane-rich stream; and an expansion valve disposed downstream of the second heat exchanger and upstream of the hydrogen stripping column and configured to expand the cooled methane-rich stream to a pressure less than or equal to about 100 psia. Such embodiments may also include a recycle circuit configured to recycle the hydrogen rich gaseous overhead from the hydrogen stripping column back to the hydrogen, nitrogen, methane and argon containing feed stream or the conditioned feed stream. A hydrogen compressor may be disposed within the recycle circuit upstream of the feed stream and configured to compress the hydrogen rich gaseous overhead stream to a pressure greater than or equal to the pressure of the hydrogen, nitrogen, methane and argon containing feed stream or the conditioned feed stream. In such embodiments, the hydrogen enriched gaseous overhead from the hydrogen stripping column is preferably warmed in the heat exchanger via indirect heat exchange with the hydrogen, nitrogen, methane and argon containing feed stream.

In embodiments that include nitrogen recovery, the present systems include a nitrogen rectification column configured to receive the vaporized or partially vaporized hydrogen free methane-rich stream and a nitrogen reflux stream and produce a nitrogen containing overhead vapor stream substantially free of methane and hydrogen, and a methane enriched liquid bottom stream. The resulting methane enriched liquid bottom stream is preferably warmed in the heat exchanger via indirect heat exchange with the feed stream to produce the methane fuel gas while the nitrogen containing overhead vapor stream substantially free of methane and hydrogen is also warmed in the heat exchanger via indirect heat exchange with the feed stream to produce a warm nitrogen stream. The warmed nitrogen stream is then directed to a nitrogen recovery system, such as a liquefier, or purification system configured to produce at least one nitrogen product, preferably a liquid nitrogen stream or a purified gaseous nitrogen stream.

In embodiments that include argon recovery, the present systems further comprises an argon rectification column configured to receive an argon enriched stream substantially free of methane from an intermediate location of the nitrogen rectification column and produce an argon bottoms liquid stream and a nitrogen enriched overhead stream. The nitrogen enriched overhead stream is then returned to the nitrogen rectification column while the argon bottoms liquid stream is extracted from the argon rectification column as a crude argon product stream.

For sake of clarity, many of the reference numerals used inFIGS. 1-5are similar in nature such that the same reference numeral in one figure corresponds to the same item, element or stream as in the other figures.

DETAILED DESCRIPTION

The following detailed description provides one or more illustrative embodiments and associated methods for cryogenic purification of a feed stream comprising hydrogen, nitrogen, methane and argon into its major constituents. The various embodiments include: (i) a cryogenic purifier system with stripping of excess hydrogen and recycling of the stripped hydrogen to the feed stream so as to increase the synthesis gas production; (ii) a cryogenic purifier system with enhanced recovery of nitrogen; (iii) a cryogenic purifier system with enhanced recovery of nitrogen and argon; and (iv) a cryogenic purifier system with an integrated nitrogen liquefier. Each of these embodiments will be described in the paragraphs that follow.

Cryogenic Purifier with Recycled Hydrogen Stream

Turning now toFIG. 1, a schematic representation of an integrated cryogenic purification system10is shown. As seen therein, a pre-purified feed stream12comprising hydrogen, nitrogen, methane and argon at a pressure greater than about 300 psia is cooled to a temperature near saturation in a primary heat exchanger20. The resulting conditioned feed stream18is directed to a synthesis gas rectification column30that is configured to produce a hydrogen and nitrogen enriched overhead vapor stream34and a methane-rich condensed phase stream32proximate the bottom of the synthesis gas rectification column30. In ammonia plant applications that employ the cryogenic purification system, the hydrogen and nitrogen enriched overhead vapor stream34would preferably have a hydrogen to nitrogen ratio of about 3:1. Also, as discussed in more detail below, the pre-purified feed stream12may be combined with a compressed hydrogen recycle stream14upstream of the heat exchanger20and the resulting high pressure mixed feed stream16comprising hydrogen, nitrogen, methane and argon is cooled to near saturation.

The conditioning of the feed streams may further include additional compression, expansion, cooling, condensing and/or vaporizing steps depending upon the source of the feed streams. Likewise, pre-purification of the feed streams preferably includes removing selected contaminants from the feed stream in an adsorption based pre-purifier (not shown). For example, in some applications residual carbon oxide impurities at levels less than about 10.0 ppm or other unwanted impurities and low boiling contaminants may accompany the crude feed stream. In such circumstances, adsorbents, getters or other purification systems (not shown) can be employed to further remove such impurities and low boiling contaminants from the crude feed streams, which could be, for example, a crude synthesis gas from an ammonia plant. Such pre-purification may be conducted while a portion of the crude feed stream is in the liquid phase or predominately gas phase and either upstream, downstream or in conjunction with the conditioning of the feed streams.

A portion of the methane rich condensed phase stream32from the bottom of the synthesis gas rectification column30is then extracted as stream35and directed to a hydrogen stripping column40configured to strip hydrogen from the methane rich condensed phase stream35and produce a hydrogen free methane bottom stream42and a hydrogen enriched gaseous overhead44.

In the illustrated embodiment, the portion of the methane rich condensed phase stream35is first subcooled in subcooler37via indirect heat exchange with a diverted first portion46of the hydrogen free methane bottom stream42. The subcooled methane rich stream38is expanded or flashed to a lower pressure by expansion valve39to a pressure less than or equal to about 100 psia with the lower pressure methane rich stream41introduced proximate the top of the hydrogen stripping column40. The warmed first portion48of the of the hydrogen free methane bottom stream is then reintroduced into the hydrogen stripping column40.

A second portion45of the hydrogen free methane bottom stream42is extracted from the hydrogen stripping column40, expanded in valve49and directed as stream47to a condenser-reboiler disposed within the synthesis gas rectification column30where it is vaporized against a working fluid such as a nitrogen rich liquid to produce a vaporized or partially vaporized hydrogen free methane-rich stream51. While the present Figures illustrate the vaporization of the hydrogen-free methane bottom stream occurring in a condenser-reboiler disposed within the synthesis gas rectification column, it is also contemplated to employ a separate, stand-alone vaporizer or perhaps integrate the vaporization step within other heat exchangers within the cryogenic purification system10. In the embodiment ofFIG. 1, the partially vaporized hydrogen free methane-rich stream51is directed to phase separator70where it is separated into a vapor phase stream74and a liquid phase stream72to facilitate feed distribution into the heat exchanger, as optimal distribution of a two phase stream directly into the heat exchanger is difficult and often leads to poor heat exchanger performance. The vapor phase stream74and liquid phase stream72(collectively stream76) are then directed to heat exchanger20where the stream(s) are further warmed via indirect heat exchange with the mixed feed stream16to produce a methane containing fuel gas stream24.

The hydrogen enriched gaseous overhead44from the hydrogen stripping column40is recycled as stream43via valve25and warmed in the heat exchanger20. The warmed hydrogen recycle stream22is preferably recompressed in compressor15and the compressed recycle stream14is combined with the pre-purified feed stream12. Alternatively, the hydrogen recycle stream may be cooled separately and introduced as a separate stream into the base of the synthesis gas rectification column30. Further alternatives contemplate combining the hydrogen enriched gaseous overhead44from the hydrogen stripping column40with other fuel gas streams such as the partially vaporized hydrogen free methane-rich stream51and further processed as described above to produce the warmed fuel gas stream24.

The hydrogen and nitrogen enriched overhead vapor stream34is taken from the synthesis gas rectification column30as a stream36and directed to heat exchanger20where it is warmed via indirect heat exchange with the mixed feed stream16to produce the hydrogen and nitrogen containing synthesis gas stream26. As indicated above, in applications involving ammonia synthesis, the hydrogen to nitrogen ratio in the hydrogen and nitrogen enrich overhead vapor stream and the hydrogen and nitrogen containing synthesis gas stream is preferably about 3:1.

For purposes of adding refrigeration to the cryogenic purification process, a cryogenic refrigeration stream80may be introduced into the process. The cryogenic stream80is preferably comprised of liquid nitrogen, but may also contain or comprise other cryogen refrigerants (e.g. CH4, Ar, etc.). In lieu of the supplemental refrigeration stream, it is possible to produce the supplemental refrigeration using a turbine, however such optional use of a separate turbine to produce the required refrigeration requires additional capital costs.

Cryogenic Purifier with Enhanced Nitrogen Recovery

Turning now toFIGS. 2 and 3, there is shown embodiments of a cryogenic purifier system and method with enhanced recovery of nitrogen both with upstream hydrogen stripping (FIG. 2) and without upstream hydrogen stripping (FIG. 3).

The integrated cryogenic purification systems10shown inFIG. 2andFIG. 3include the pre-purified feed stream12, compressed hydrogen recycle stream14, high pressure mixed feed stream16, conditioned feed stream18, synthesis gas rectification column30, hydrogen and nitrogen enriched overhead vapor stream34, methane-rich condensed phase stream32as generally shown and described with reference toFIG. 1, and for sake of brevity will not be repeated here. Also, like the embodiment ofFIG. 1, the hydrogen and nitrogen enriched overhead vapor stream34ofFIGS. 2 and 3are also taken from the synthesis gas rectification column30as stream36and directed to heat exchanger20where it is warmed via indirect heat exchange with the mixed feed stream16to produce the hydrogen and nitrogen containing synthesis gas stream26. Preferably, the hydrogen to nitrogen ratio in the hydrogen and nitrogen enrich overhead vapor stream and the hydrogen and nitrogen containing synthesis gas stream is about 3:1.

In addition, the embodiment shown inFIG. 2also includes the methane rich stream35, the hydrogen stripping column40, the hydrogen free methane bottom stream42, the hydrogen enriched gaseous overhead44, the subcooler37, the subcooled methane rich stream38, the expanded methane rich stream41as well as the diverted first portion46of the hydrogen free methane stream42and subsequently warmed first portion48of the of the hydrogen free methane stream that are extracted from and reintroduced into the hydrogen stripping column40, respectively. These elements and features of the illustrated embodiment are similar to or identical to the corresponding features shown and described with reference to the embodiment ofFIG. 1.

In the embodiment ofFIG. 2, the hydrogen enriched gaseous overhead44from the hydrogen stripping column40is preferably recycled as stream43via valve25and warmed in the heat exchanger20. The warmed hydrogen recycle stream22is then recompressed in compressor15and the compressed recycle stream14is combined with the pre-purified feed stream12in a manner similar to that described above with reference toFIG. 1. Alternatively, the hydrogen enriched gaseous overhead44from the hydrogen stripping column40may be combined with other fuel gas streams and further processed as described above to produce the warmed fuel gas stream24.

The main difference between the embodiment shown inFIG. 1and the embodiment shown inFIG. 2relates to the enhanced recovery of nitrogen. As taught above with reference toFIG. 1, a second portion45of the hydrogen free methane bottom stream42is extracted and directed via valve49as stream47to a condenser-reboiler disposed within the synthesis gas rectification column30where it is partially vaporized against the synthesis gas rectification column overhead to produce a partially vaporized hydrogen free methane-rich stream51.

In the embodiment ofFIG. 2, this partially vaporized hydrogen free methane-rich stream51, is directed to a nitrogen rectification column50configured to produce a nitrogen containing overhead vapor stream54substantially free of methane and hydrogen, and a methane enriched liquid bottom stream52. To facilitate the rectification within the nitrogen rectification column50, a liquid nitrogen reflux stream53is also introduced to the nitrogen rectification column50. The liquid nitrogen stream80preferably comes from an integrated nitrogen liquefier (SeeFIG. 5) where a diverted portion83of the liquid nitrogen stream80is introduced via valve85as liquid nitrogen reflux stream53to the upper portion of the nitrogen rectification column50. Alternatively, the liquid nitrogen stream80may be derived from a remote liquid nitrogen source such as a remote liquid storage tank or reservoir (not shown).

A key aspect or feature of the present embodiment that enables a large fraction of the nitrogen to be recovered is the use of a mechanical liquid pump for the re-pressurization of the methane enriched liquid bottoms taken from the nitrogen rectifier. The nitrogen rectification column preferably operates at a pressure below the fuel gas header pressure, for example, at a pressure of less than or equal to about 50 psia, and more preferably at a pressure of less than or equal to about 25 psia. Alternatively, the use of a compressor to re-compresses the warmed (i.e. vaporized) methane back to the pressure of the fuel gas header may be used in lieu of the mechanical liquid pump.

The nitrogen containing overhead vapor stream56is warmed in heat exchanger20and the warmed nitrogen containing vapor stream28is directed to a nitrogen recovery system (not shown inFIGS. 2 and 3) to produce at least one nitrogen product, such as a gaseous nitrogen product and/or a liquid nitrogen product. A portion of the methane rich liquid bottom stream52is extracted from the nitrogen rectification column50as a methane rich stream55which is pumped to an appropriate pressure and warmed in the heat exchanger20to produce the methane fuel gas24. Preferably, the pumped methane rich stream55together with the optional hydrogen vapor stream43(shown inFIG. 2) and any supplemental refrigeration stream80is directed to the phase separator70where it is separated into a vapor phase stream74and a liquid phase stream72(collectively stream76) and directed to heat exchanger20where it is warmed via indirect heat exchange with the mixed feed stream16to produce the methane containing fuel gas24. The phase separator70(shown inFIG. 2) is an optional item in that it may not be needed in embodiments of the present system that only direct methane liquid and/or liquid nitrogen to the heat exchanger (SeeFIG. 3). The main difference between the embodiment shown inFIG. 2and the embodiment shown inFIG. 3relates to the hydrogen stripping column and the hydrogen recycling circuit. In the embodiment ofFIG. 3, the hydrogen stripping column and hydrogen recycling circuit are absent such that the hydrogen containing, methane rich stream35extracted from the synthesis gas rectification column30is directed via valve49as stream47to a condenser-reboiler disposed within the synthesis gas rectification column30where it is partially vaporized. This partially vaporized hydrogen and nitrogen containing methane-rich stream51A is directed to a nitrogen rectification column50along with a liquid nitrogen reflux stream53where it is separated to produce a nitrogen and hydrogen containing overhead vapor stream54substantially free of methane, and a methane enriched liquid bottom stream52.

The nitrogen and hydrogen containing overhead vapor stream56is warmed in heat exchanger20and directed to a nitrogen and hydrogen recovery system (not shown) to either separate the nitrogen and hydrogen as separate products or to reintroduce the N2—H2mixture into the NH3synthesis train. Similar to the embodiment ofFIG. 2, a portion of the methane rich liquid bottom stream52is extracted from the nitrogen rectification column50as a methane rich stream55typically at a pressure of between about 15 psia and 25 psia which is pumped to an appropriate pressure of preferably between about 30 psia to 40 psia or higher pressures, and subsequently warmed in the heat exchanger20to produce the methane fuel gas24.

Cryogenic Purifier with Enhanced Nitrogen and Argon Recovery

Turning now toFIG. 4, there is shown another embodiment of a cryogenic purifier system and method similar to that shown inFIG. 2but with enhanced recovery of both nitrogen and argon.

In many regards, the embodiment shown inFIG. 4is very similar to the embodiment shown inFIG. 2, described above. The key difference between the embodiment shown inFIG. 4and the embodiment shown inFIG. 2relates to the enhanced recovery of argon using an argon rectification column60operatively coupled to the nitrogen rectification column50. Preferably, an argon enriched stream67is extracted from an intermediate location of the nitrogen rectification column50and preferably at a location that is substantially free of methane, for example at a location where the methane concentration is less than about 1.0 part per million (ppm) and more preferably less than about 0.1 ppm. The extracted argon enriched stream67may be a liquid stream, a gaseous stream, or a two phase stream comprising a fraction of liquid argon and a fraction of gaseous argon.

The extracted argon enriched stream67is directed to an argon rectification column60preferably operating at a pressure of between about 65 psia and 80 psia and configured to separate the argon enriched stream and produce an argon bottoms liquid stream62and a nitrogen enriched overhead stream66. The nitrogen enriched overhead stream66is subsequently returned to the nitrogen rectification column50at a location preferably above the intermediate location where the argon enriched stream67is extracted. The argon rectification column60further includes a condenser-reboiler65configured to reboil argon rectification column60. A portion of the descending argon liquid within the column60is vaporized in condenser-reboiler65against a stream of condensing gaseous nitrogen the resulting liquid nitrogen stream68may then be directed to the top of column50. Although pressurized nitrogen, such as a compressed portion of nitrogen stream56after warming, is the preferred fluid to supply the reboil duty for argon rectification column60other fluids could also be employed. The resulting argon bottoms liquid stream62from argon rectification column60is removed and could be taken directly as a crude argon merchant product or transported to a separate or an offsite argon refinement process, where it could later be further purified into suitable high purity argon product.

The liquid nitrogen stream68is preferably combined with liquid reflux stream83. A first diverted portion of the liquid nitrogen stream80is a nitrogen reflux stream53introduced into the nitrogen rectification column50. Reflux for column50may also be supplemented with the condensed nitrogen derived from condenser-reboiler65. A second diverted portion of the liquid nitrogen stream80can optionally be diverted as stream84and used to supplement the refrigeration of the present purification process independent of the operation of the rectification column50.

While the preferred embodiment of the cryogenic purification system and process with nitrogen and argon recovery is described with reference toFIG. 4, alternative embodiments are contemplated where the upper portion of nitrogen rectification column may be configured atop the argon rectification column. In this alternate configuration, the bottom half of the nitrogen column might be a separate column or may even be configured as a divided wall column.

Cryogenic Purifier with an Integrated Nitrogen Liquefier

Turning now toFIG. 5, there is shown an integrated nitrogen liquefier arrangement100suitable for use in the cryogenic purifier systems10ofFIGS. 1-4. As seen therein, the incoming stream28is preferably the warmed nitrogen containing vapor stream received from the above-described cryogenic purifier system10and compressed in a multi-stage compressor arrangement (shown inFIG. 5as compressor stages102,104). The compressed nitrogen stream105is optionally further compressed in a turbine loaded booster compressor106.

A first portion107of the further compressed nitrogen vapor stream is diverted from the booster compressor106to a refrigeration circuit where the first portion107is cooled via indirect heat exchange in economizer115with a refrigerant stream118. The warmed refrigerant stream116is routed back to a chiller117where it is cooled and recycled back to the economizer115in a generally closed loop fashion. The diverted and cooled first portion108of the further compressed nitrogen stream is then expanded in turboexpander130with the resultant exhaust stream109directed to the heat exchanger120to supply supplemental refrigeration to the integrated nitrogen liquefier arrangement and subsequently returned as warmed exhaust stream121to an intermediate stage of the multi-stage compressor arrangement102/104, as preferably shown inFIG. 5.

A second portion111of the further compressed nitrogen stream is directed to the heat exchanger120. Part of the second portion111of the further compressed nitrogen stream is only partially cooled in the heat exchanger120and diverted as stream112to the turbine110that drives the turbine loaded booster compressor. The remaining part of the second portion111of the further compressed nitrogen stream is fully cooled in the heat exchanger120, valve expanded in expansion valve125to form a second liquid or partially liquid nitrogen stream126.

The resulting expanded nitrogen stream114is optionally directed to a condenser-reboiler130to condense or partially condense nitrogen stream114to form a first liquid or partially liquid nitrogen stream124. The objective of the condenser-reboiler130is optionally supply the reboil stream necessary to operate argon stripping column60(SeeFIG. 4). In this regard, condenser-reboiler130is the same as reboiler65ofFIG. 4. Alternatively, the reboil stream can be extracted from feed gas compressor102and directed in a separate pass into the reboiler65ofFIG. 4.

The liquid or partially liquid nitrogen streams124,126are preferably mixed and directed as a combined stream to a first phase separator140configured to produce a liquid nitrogen stream142and a cold gaseous nitrogen stream144. The cold gaseous nitrogen stream144is sent to the heat exchanger120to recover some refrigeration and the resulting warmed stream123is preferably mixed with the warmed exhaust stream121and recycled back to an intermediate stage of the multi-stage compressor arrangement102/104. Recycling of the warmed exhaust stream121and/or the warmed stream123may be to an intermediate stage of the multi-stage compressor arrangement102/104(shown inFIG. 5) or perhaps to a location upstream or downstream of the multi-stage compressor arrangement102/104will depend on the pressures of the warmed exhaust stream121and warmed stream123.

The liquid nitrogen stream142extracted from the first phase separator140is valve expanded in expansion valve145and directed to a second phase separator150configured to produce a liquid nitrogen product stream152and a cold gaseous nitrogen stream154that may be warmed and recycled back to incoming stream28after some or all of its refrigeration is recovered in heat exchanger120. A stream of cold nitrogen vapor155may further represent an additional integration point between the liquefier100and the cryogenic purification system10. If the argon and hydrogen has been previously recovered in the cryogenic purification system10, the liquid nitrogen product stream152and the gaseous nitrogen stream154will be purified. On the other hand, if the argon and/or hydrogen has not been previously recovered in the cryogenic purification system10, the liquid nitrogen product stream152and the gaseous nitrogen stream154may contain measurable levels of argon and/or hydrogen which can and should be recovered within the liquefaction arrangement100or in a separate upstream or downstream recovery process.

With respect to the above-described integrated nitrogen liquefier arrangement100, it is also possible to incorporate multiple stages of compression and/or use multiple compressors arranged in parallel for purposes of accommodating multiple return pressures of the recycled streams. In addition, the turbo-expanded refrigerant stream109may be directed to an intermediate location of the heat exchanger120(e.g. with respect to temperature) as the turbine discharge or exhaust does not have to be near saturation. The shaft work of expansion from turbine135and/or turbine110can be directed to various compressors in other process streams within the integrated cryogenic purification system10or, as shown with respect to turbine110may be used to “self-boost” the expansion stream. Alternatively, the shaft work of expansion from turbine135and/or turbine110may also be loaded to a generator.

INDUSTRIAL APPLICABILITY

As integrated with an ammonia synthesis process in an ammonia production plant, the present cryogenic purifier system and method takes a crude feed stream comprising hydrogen, nitrogen, methane and argon and produces the following product streams: (i) a hydrogen-nitrogen synthesis gas stream that may be recycled back to the ammonia plant synthesis section, and more particularly the ammonia synthesis gas stream upstream of the compressor or of the ammonia plant; (ii) a high methane content fuel gas that may be recycled back to the ammonia production plant and preferably to the steam reforming section of the ammonia plant, and more specifically to the furnace by which the primary reformer is fired; (iii) a liquid argon product stream; and (iv) a substantially pure nitrogen gaseous stream which may be recycled back to the ammonia plant, taken as a gaseous nitrogen product, or more preferably directed to a nitrogen recovery system, such as the liquefier as described above, to produce liquid and gaseous nitrogen products. The operating costs associated with the present integrated cryogenic purifier system and method are substantially lower that a Braun Purifier system or other conventional cryogenic purification systems.

While the present invention has been described with reference to one or more preferred embodiments and operating methods associated therewith, it should be understood that numerous additions, changes and omissions to the disclosed system and method can be made without departing from the spirit and scope of the present invention as set forth in the appended claims.