US20060239871A1 - Low pressure drop purifier for nitrogen, methane, and argon removal from syngas - Google Patents
Low pressure drop purifier for nitrogen, methane, and argon removal from syngas Download PDFInfo
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- US20060239871A1 US20060239871A1 US11/472,590 US47259006A US2006239871A1 US 20060239871 A1 US20060239871 A1 US 20060239871A1 US 47259006 A US47259006 A US 47259006A US 2006239871 A1 US2006239871 A1 US 2006239871A1
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Abstract
An apparatus for purifying a raw syngas stream containing excess nitrogen and an ammonia process plant for manufacturing ammonia from syngas with excess air for reforming and nitrogen removal with low pressure losses is disclosed. Auto-refrigeration for cooling the syngas for cryogenic hydrogen enrichment is provided by expansion of a hydrogen-lean waste fluid stream from a distillation column
Description
- The present application is a divisional to co-pending U.S. patent application Ser. No. 10/604,404, filed on Jul. 17, 2003.
- The present embodiments relate generally to methods and apparatus to improve production of synthesis gas for manufacturing ammonia. The present embodiments reduces pressure losses in a nitrogen-wash purifier unit
- Processes for manufacturing ammonia from a hydrocarbon and air, via a hydrogen/nitrogen synthesis gas (syngas), are well known. Extraneous syngas components typically include inert gases from the air and/or the hydrocarbon feed, such as argon and methane. When excess air is used in the syngas production, nitrogen is also present in stoichiometric excess, and must be removed from a raw makeup syngas stream or purged from an ammonia synthesis loop to maintain a desired ammonia synthesis reactor feed composition.
- In the prior art, some syngas production methods use excess air and cryogenic syngas purification, which relies on a syngas pressure drop upstream of purification for refrigeration. The pressure drop is subsequently made up in a compressor that raises the syngas to ammonia synthesis loop pressure. This type of method also reduces the rate of recycle or purge gas flow from the ammonia reactor loop due to the upstream removal from the makeup syngas of inerts such as argon and methane in the syngas purification.
- Other methods of ammonia synthesis use high-activity catalyst in the ammonia synthesis reactor. Purge gases are eliminated via a hydrogen enrichment process operating on a sidestream of the syngas recycled to the synthesis loop compressor. The total recycle flow is roughly three times the volumetric flowrate of the makeup syngas.
- Other methods use air separation to provide oxygen-enriched air such that reforming produces a synthesis gas with higher hydrocarbon slip than in other ammonia manufacturing systems. A higher concentration of nonreactive gas in the ammonia synthesis is managed by purging from a residual syngas stream following recovery of ammonia product. This type of method unloads front-end gas reforming reactors, at the expense of including air separation, but ostensibly enables a smaller purge stream process after ammonia synthesis.
- Other methods are centered on an integrated process system for synthesizing methanol and ammonia that uses a nitrogen wash by cryogenic fractionation to purify ammonia syngas, with refrigeration supplied externally and providing no recovery of expansion power in the process.
- The present embodiments meet these needs.
- The detailed description will be better understood in conjunction with the accompanying drawings as follows:
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FIG. 1 is a schematic process flow sheet showing prior art syngas purification using an upstream syngas feed to drive an expander and extract syngas energy as work to achieve auto-refrigeration. -
FIG. 2 is a schematic process flow sheet of an embodiment of the present invention, using expansion of a nitrogen-rich liquid waste stream to generate auto-refrigeration in the process. -
FIG. 3 is a schematic process flow sheet showing an alternate embodiment of the present invention wherein syngas feed or liquefied waste gas can be expanded across a liquid expander for refrigeration. -
FIG. 4 is a block flow diagram of an embodiment of the invention showing low pressure drop nitrogen removal integrated in an ammonia synthesis process with secondary reforming with excess air and heat-exchanging reforming. -
FIG. 5 is block flow diagram of an alternative embodiment of the invention showing low pressure drop nitrogen removal integrated in an ammonia synthesis process with conventional primary steam reforming and secondary reforming with excess air - The present embodiments are detailed below with reference to the listed Figures.
- Before explaining the present embodiments in detail, it is to be understood that the embodiments are not limited to the particular embodiments and that they can be practiced or carried out in various ways.
- The present embodiments provide methods to purify syngas. Syngas, as an example, occurs in ammonia manufacturing processes. The methods use cryogenic distillation to purify syngas, and obtain refrigeration for the distillation from waste fluid expansion using a liquid expander to recover mechanical work from the waste fluid. These methods reduce the pressure losses in the syngas stream and concomitantly reduce compression costs and power relative to similar prior art ammonia processes utilizing nitrogen and inerts removal.
- The methods are applicable in grassroots plant design, and can also be applied to retrofit existing synthesis gas systems to improve process performance and economics. In the retrofit, for example, the lower pressure drop of the present embodiments can allow process modification for reforming with excess air and nitrogen removal from the makeup syngas without expensive modification or replacement of the synthesis loop and/or makeup gas compressors.
- In an embodiment, the present embodiments provide methods to purify syngas, including: (a) introducing a raw syngas stream containing excess nitrogen to a feed zone in a distillation column; (b) expanding a liquid bottoms stream from the distillation column through a liquid expander with a work output to form a cooled waste fluid stream; (c) rectifying vapor from the feed zone in the distillation column to form an overhead vapor stream of reduced nitrogen and inerts content; (d) cooling the overhead vapor stream in indirect heat exchange with the cooled waste fluid stream to form a partially condensed overhead stream and a relatively warm waste fluid stream; (e) separating the partially condensed overhead stream into a condensate stream and a purified syngas vapor stream of reduced nitrogen and inerts content; and (f) refluxing the distillation column with the condensate stream. The method can also include cooling the raw syngas stream by expansion across a Joule-Thompson (J-T) valve in advance of the introduction to the feed zone. Additionally, the method can include cooling the raw syngas stream in cross-exchange against the warm waste fluid stream and against the purified syngas vapor stream. In this embodiment, adjusting the flow to the liquid bottoms stream expansion controls liquid level in the distillation column.
- The methods can further include producing the raw synthesis gas by reforming a hydrocarbon, wherein the reforming includes autothermal or secondary reforming with excess air. The purified syngas vapor stream can be supplied to an ammonia synthesis loop for manufacturing ammonia.
- In an embodiment, the present embodiments provide an ammonia process. The process embodiments include reforming a hydrocarbon to form syngas. The reforming can include autothermal or secondary reforming with excess air to form a raw syngas stream containing excess nitrogen for ammonia synthesis. The process embodiments include cooling the raw syngas stream in a cross-exchanger and expanding the cooled raw syngas stream. The expanded raw syngas stream is introduced to a feed zone in a distillation column. The liquid bottoms stream from the distillation column is expanded through a liquid expander to form a cooled waste fluid stream. The process embodiments include rectifying vapor from the feed zone in the distillation column to form an overhead vapor stream of reduced nitrogen and inerts content. The overhead vapor stream is cooled in indirect heat exchange with the cooled waste fluid stream to form a partially condensed overhead stream and a partially warmed waste fluid stream. The partially condensed overhead stream is separated into a condensate stream and a purified syngas vapor stream of reduced nitrogen and inerts content. The distillation column is refluxed with the condensate stream and the purified syngas vapor stream and the partially warmed waste fluid stream are heated in one or more cross-exchangers. The purified syngas vapor stream is supplied from the cross-exchanger to an ammonia synthesis loop.
- In an embodiment, the present embodiments can be applied to improve an ammonia process that includes the steps of reforming a hydrocarbon with excess air to form a raw syngas stream, removing nitrogen and inerts from the raw syngas stream by distillation. The cooling can be provided by process fluid expansion through an expander-generator, wherein an overhead stream is partially condensed against a waste stream cooled by expanding bottoms liquid from a distillation column, and supplying syngas with reduced nitrogen and inerts content from the distillation to an ammonia synthesis loop. The process embodiments can include optionally expanding the raw syngas stream across a Joule-Thompson valve upstream of the distillation column; and/or expanding the bottoms liquid through a liquid expander with a work output.
- In an embodiment, the present embodiments provide for a purification apparatus for purifying a raw syngas stream containing excess nitrogen. The embodied apparatus, can include means for introducing the raw syngas stream to a feed zone in a distillation column; means for expanding a liquid bottoms stream from the distillation column to form a cooled waste fluid stream; means for rectifying vapor from the feed zone in the distillation column to form an overhead vapor stream of reduced nitrogen and inerts content; means for cooling the overhead vapor stream in indirect heat exchange with the cooled waste fluid stream to form a partially condensed overhead stream and a relatively warm waste fluid stream; means for separating the partially condensed overhead stream into a condensate stream and a purified syngas vapor stream of reduced nitrogen and inerts content; and means for refluxing the distillation column with the condensate stream.
- In an embodiment, the present embodiments provide for an ammonia process plant. The embodied an ammonia process plants can include means for reforming a hydrocarbon to form syngas, wherein the reforming means includes an autothermal or secondary reformer and means for supplying excess air to the autothermal or secondary reformer, to form a raw syngas stream containing excess nitrogen for ammonia synthesis; cross-exchanger means for cooling the raw syngas stream; means for expanding the cooled raw syngas stream from the cross-exchanger; means for introducing the expanded raw syngas stream to a feed zone in a distillation column; means for expanding a liquid bottoms stream from the distillation column through a liquid expander to form a cooled waste fluid stream; means for rectifying vapor from the feed zone in the distillation column to form an overhead vapor stream of reduced nitrogen and inerts content; means for cooling the overhead vapor stream in indirect heat exchange with the cooled waste fluid stream to form a partially condensed overhead stream and a partially warmed waste fluid stream; means for separating the partially condensed overhead stream into a condensate stream and a purified syngas vapor stream of reduced nitrogen and inerts content; means for refluxing the distillation column with the condensate stream; means for heating the purified syngas vapor stream in the cross-exchanger; means for heating the partially warmed waste fluid stream in the cross exchanger; and means for supplying the purified syngas vapor stream from the cross-exchanger to an ammonia synthesis loop
- With reference to the figures,
FIG. 1 depicts an example of prior art syngas purification PA. Asyngas feed stream 10 drives expander 12, extracting syngas energy aswork 14 to achieve auto-refrigeration. Thefeed stream 10 is chilled incross-exchangers distillation column 20. Between thecross-exchangers raw syngas 10 is expanded in aturboexpander 12, cooling theraw syngas 10 and recoveringwork 14. Theexpander 12 can be bypassed or supplemented by using a Joule-Thompson (J-T)valve 22, for example during startup. The partially liquefiedraw syngas 13 from the cross-exchanger 18 enters thedistillation column 20 to be further cooled, partly condensed, and rectified, yielding apurified syngas stream 24 of lowered nitrogen and inerts content and a hydrogen-leanwaste gas stream 26. The purifiedsyngas stream 24 andwaste gas stream 26 pass through the cross-exchangers 16, 18 to chill the rawsyngas feed stream 10 as mentioned previously. - The
waste gas stream 26 is discharged from thedistillation column 20 as bottoms stream 28, flashed acrosslevel control valve 30, and used as a coolant in aheat exchanger 32 integral with thedistillation column 20. Theheat exchanger 32 cools and partially condenses overhead vapor from thecolumn 20 to obtain syngas liquid to reflux thecolumn 20. Themakeup syngas stream 24 is compressed for conversion in ammonia synthesis reactors (not shown) that operate at higher pressures. Thus, a pressure drop incurred by theraw syngas 10 in the purification PA must be recouped downstream by consuming additional power for compression. -
FIG. 2 depicts an embodiment ofsyngas purification 34 using mechanical expansion of the liquid bottoms stream 28 to generate a major fraction of the auto-refrigeration in thepurification process 34. Asingle cross-exchanger 36 is used in place of the cross-exchangers 16, 18 ofFIG. 1 , although cross-exchanger 36 can include a plurality of physical stages. Theraw syngas stream 10 is passed throughvalve station 38 upstream of thedistillation column 20. Thevalve station 38 can include a primary, line-size valve for flow during normal operation, and a J-T secondary valve for trim and/or startup for auto-refrigeration. Theraw syngas stream 10 then enters aninlet zone 40 of thecolumn 20, preferably as a mixture of syngas vapor and liquid. In theinlet zone 40, syngas liquid separates and is collected inliquid holdup zone 42. The liquid exits thecolumn 20 as bottoms stream 28 via alower outlet 44. The column bottoms stream 28 is expanded through aliquid expander 46 to auto-refrigerate thebottoms 28 and recoverwork 48, which can be used to drive a pump, compressor, electrical generator, or the like. As used herein, a “liquid expander” is a work-output device that receives a liquid supply and produces a liquid or vapor effluent, preferably a mixed vapor-liquid effluent. Where the effluent fluid is liquid, theliquid expander 46 can be a hydraulic turbine. - A
bypass J-T valve 50 is included for gas or two-phase flow, e.g. at startup. In operation, expansion of the bottoms stream 28 is preferably a primary source of auto-refrigeration in thesyngas purification process 34 of the present embodiments, whereas the expansion across the bypass J-T valve atvalve station 38 is a relatively minor source. The bypass J-T valve can be a significant refrigeration source during startup. - From
liquid expander 46, the chilledwaste fluid stream 28 enters acoolant inlet 52 of an indirectheat exchange zone 32 integral to thecolumn 20. The flow rate to theliquid expander 46 controls the liquid level in theholdup zone 42 and also, in part, regulates conditions in thecolumn 20, based on feedback from asyngas analyzer 56. Conditions in thecolumn 20 determine the composition of the purifiedsyngas stream 24. For example, more refrigeration reduces the nitrogen content; less refrigeration increases the nitrogen content. The chilledwaste fluid stream 28 passes through theheat exchange zone 32, discharging from thecolumn 20 viacoolant outlet 56. During transit through theheat exchange zone 32, the bottoms stream 28 cools and partially condenses overhead vapor from thecolumn 20. - From the
inlet zone 40, syngas vapor flows upward through acontact zone 58 in contact with liquid flowing downward through thecontact zone 58 to absorb nitrogen and enrich the hydrogen content of the vapor. At the upper end of thecontact zone 58, the vapor enters avapor riser 60 and flows to avapor inlet zone 62 at an upper end of theheat exchange zone 32. The vapor passes tube-side through theheat exchange zone 32 for partial condensation against thewaste fluid stream 28, further enriching the vapor in lower-boiling components. Vapor and condensate exit theheat exchange zone 32 and are separated in aknockout zone 64. Vapor exits thecolumn 20 as the purifiedsyngas stream 24, discharging viasyngas outlet 66. The condensate collects in a liquid seal well 68 below theknockout zone 64 and in communication with thecontact zone 58. The condensate overflows from the seal well 68 to flow downward through thecontact zone 58 to theliquid holdup zone 42 as described previously. -
FIG. 3 depicts another embodiment of asyngas purification process 70, in which the process PA ofFIG. 1 can be modified or retrofitted according to the present embodiments. A bottomsliquid expander 46 is added to auto-refrigerate the bottoms stream 28 by recovering work, for example aspower 48. Abypass J-T valve 50 is also installed, as inFIG. 2 . The resultingretrofit purification process 70 is comparable to the inventive embodiment ofFIG. 2 , but can also be operated in the original configuration, if desired. For low pressure drop operation, theoriginal syngas turboexpander 12 is bypassed and thevalve 22 is set full open, or optionally bypassed (not shown). - In an embodiment, expansion of a liquid byproduct stream of purged gases (such as, the column bottoms stream 28) can generate a major portion of the auto-refrigeration required for the purification process. This generation avoids a major part of the syngas pressure loss incurred in the prior art configuration of
FIG. 1 . In the prior art process PA, a pressure drop of about 3.1 bars typically occurs from introduction of thesyngas feed stream 10 to exit of the purifiedsyngas stream 24. Most of this pressure drop occurs across theexpander 12, which drops the raw syngas pressure by about 1.8 to 2.0 bar. In an embodiment as exampled inFIG. 2 , a pressure drop from introduction of thesyngas feed stream 10 to exit of the purifiedsyngas stream 24, can be limited to a range of about 0.75 to 1.3 bar by obtaining a major portion of the required auto-refrigeration effect from expansion of the column bottoms stream 28 instead of from the rawsyngas feed stream 10. - Referring to
FIG. 4 , an embodiment of an ammonia manufacturing process can include catalytic reforming of afeed including hydrocarbon 100 andsteam 102 in a reactor/exchanger 104 of the type known under the trade designation KRES. Additional reforming of afeed including hydrocarbon 100 andsteam 102 withexcess air 106 as oxidant can be effected insecondary reformer 108. The process can include high and/or low temperature shift conversion andcarbon dioxide removal 110, methanation and drying 112,syngas purification 114 as described in reference toFIG. 2 or 3,compression 116, andammonia synthesis 118. Apurge stream 120 is recycled from theammonia synthesis 118 to upstream of the syngas purification 114 (such as, to the methanation and drying 112). Therecycled stream 120 can be relatively smaller in mass flow rate than the raw syngas stream 10 (as exampled inFIG. 2 ), for example, in a range of from about 5 weight percent to 25 weight percent of theraw syngas stream 10, and preferably in a range of from 10 to 20 weight percent of theraw stream 10. Thewaste gas stream 26 can be exported for fuel gas value. - Referring to
FIG. 5 , another embodiment of an ammonia manufacturing process can include catalytic reforming of afeed including hydrocarbon 100 andsteam 102 in a conventionalprimary reformer 122 followed by additional reforming withexcess air 106 in conventional secondarycatalytic reformer 124. Shift conversion andcarbon dioxide removal 110, methanation and drying 112,syngas purification 114,compression 116,ammonia synthesis 118 andpurge stream 120 recycle are as described in reference toFIG. 4 .Waste gas stream 26 can be burned as a fuel inprimary reformer 122 and/or exported for fuel gas as inFIG. 4 . - The purification process of
FIG. 2 can be used in a new plant for improved energy consumption and capital cost savings, or can be used to retrofit an existing purification process like that ofFIG. 1 to reduce operating costs and/or to increase capacity. The process ofFIG. 2 can be used to retrofit an existing plant that does not use purification and/or excess air. Retrofitting for reforming with excess air can increase the capacity of the existing plant and enhance the life of the tubes and/or other internals in the existing reformer(s) by shifting some of the reforming duty to the secondary reformer and lowering the operating temperature of the primary reformer. Installing nitrogen removal also allows for more flexible reforming operation (such as, higher methane slip), and less purge or recycle from the ammonia synthesis loop due to the reduction of inerts with the nitrogen removal. Nitrogen purification/excess air retrofits using the low-ΔP purification process of the present invention can improve the retrofit by reducing or eliminating the extent of modifications to the makeup syngas compressor, which can make the retrofit economically feasible for a larger number of existing ammonia plants. - The purification method of the present invention embodiment of
FIG. 2 is compared to that of the prior art inFIG. 1 . Both FIGS. 1 and, 2 process a rawsyngas feed stream 10 to produce apurified syngas stream 24 and awaste gas stream 26, and the inlet and outlet stream compositions are the same in both cases as shown in Table 1 below.TABLE 1 Purification Syngas Specifications Stream Composition, mole percent Raw Purified Waste Gas Syngas Syngas Gas Component (10) (24) (26) Hydrogen 65.8 74.7 6.6 Nitrogen 31.4 24.9 74.2 Methane 2.2 0.006 16.7 Argon 0.6 0.4 2.5 Total 100.0 100.0 100.0 - Operation of the low-ΔP process of
FIG. 2 was simulated for a 2200 metric tons per day ammonia plant to compare the operating temperatures, pressures and flow rates to those of theFIG. 1 prior art process as a base case. The results are shown in Table 2 below.TABLE 2 Purification Operating Conditions Basis: 2200 MTPD Ammonia Base Case Example Process Stream, Location ( FIG. 1 )( FIG. 2 )RAW SYNGAS (10), INLET TO CROSS-EXCHANGER (20) Temperature, ° C. 4.0 4.0 Pressure, kPa 3,479.0 3,479.0 Mass flow, kg/hr 142,124 142,124 RAW SYNGAS (10), INLET TO COLUMN (20) Temperature, ° C. −172.6 −172.0 Pressure, kPa 3,240.0 3,454.0 Mass flow, kg/hr 142,124 142,124 SYNGAS (24), OUTLET FROM COLUMN (20) Temperature, ° C. −178.6 −178.2 Pressure, kPa 3,215.0 3,429.0 Mass flow, kg/hr 99,607 99,529 SYNGAS (24), OUTLET FROM CROSS-EXCHANGER (16, 20) Temperature, ° C. 1.3 2.1 Pressure, kPa 3,165.0 3,404.0 Mass flow, kg/hr 99,607 99,529 BOTTOMS LIQUID (28), OUTLET FROM COLUMN (20) Temperature, ° C. −172.8 −172.2 Pressure, kPa 3,240.0 3,454.0 Mass flow, kg/hr 42,517 42,596 WASTE FLUID (26), INLET TO EXCHANGER (32) Temperature, ° C. −186.0 −187.6 Pressure, kPa 319.0 302.1 Mass flow, kg/hr 42,517 42,596 WASTE FLUID (26), OUTLET FROM CROSS-EXCHANGER (16, 36) Temperature, ° C. 1.3 2.1 Pressure, kPa 256.4 253.3 Mass flow, kg/hr 42,517 42,596 - The data in Table 2 show that the flow rates and temperatures are similar, but the pressure drop for the syngas between the purification process inlet and outlet is considerably lower in the
FIG. 2 example compared to theFIG. 1 base case. This will generally require less makeup gas compression to the ammonia synthesis loop pressure. The power requirements for makeup syngas compression, fluid expansion power output, and net compression and expansion were also determined for theFIG. 1 base case and theFIG. 2 example. The results are shown in Table 3 below.TABLE 3 Power Balance Basis: 2200 MTPD Ammonia Base Case Example Compression/Expansion ( FIG. 1 )( FIG. 2 )MAKEUP SYNGAS COMPRESSION, KW 8,310.66 7,453.49 RAW SYNGAS EXPANSION, KW −203.39 — WASTE FLUID EXPANSION, KW — −120.40 NET COMPRESSION/EXPANSION 8,107.27 7,333.09 POWER, KW - As seen in the data presented above, the purification process of
FIG. 2 is characterized by a lower syngas pressure drop than the prior art process ofFIG. 1 . While less power is recovered from expansion of the waste fluid in the example ofFIG. 2 than in the syngas feed expansion in the base case ofFIG. 1 , the reduction in makeup compression power is more significant. Thus, not only is the syngas pressure drop reduced, but the overall power requirements are also less, potentially resulting in both capital and operating cost savings in a new ammonia plant. In a retrofit of an existing non-purifier based ammonia plant, the reduced pressure drop of theFIG. 2 example can result in increased capacity and/or less significant or no modification of the makeup syngas compressor. - The embodiments are described above with reference to non-limiting examples provided for illustrative purposes only. Various modifications and changes will become apparent to the skilled artisan in view thereof. All such changes and modifications are intended within the scope and spirit of the appended claims and shall be embraced thereby.
Claims (17)
1) An apparatus for purifying a raw syngas stream containing excess nitrogen comprising:
means for introducing the raw syngas stream to a feed zone in a distillation column;
means for expanding a liquid bottoms stream from the distillation column through a liquid expander with a work output to form a cooled waste fluid stream;
means for rectifying vapor from the feed zone in the distillation column to form an overhead vapor stream of reduced nitrogen and inerts content;
means for cooling the overhead vapor stream in indirect heat exchange with the cooled waste fluid stream to form a partially condensed overhead stream and a relatively warm waste fluid stream;
means for separating the partially condensed overhead stream into a condensate stream and a purified syngas vapor stream of reduced nitrogen and inerts content; and
means for refluxing the distillation column with the condensate stream.
2) The apparatus of claim 1 , further comprising means for cooling and expanding the raw syngas stream across a Joule-Thompson valve in advance of the introduction to the feed zone.
3) The apparatus of claim 2 , wherein the means for expanding the liquid bottoms stream comprises a hydraulic turbine.
4) The apparatus of claim 1 , wherein the relatively warm waste fluid stream from the overhead vapor cooling consists of a vapor phase.
5) The apparatus of claim 1 , wherein the relatively warm waste fluid stream from the liquid expander comprises mixed vapor and liquid.
6) The apparatus of claim 1 , wherein a liquid level in the distillation column is controlled by adjusting flow the expansion to the liquid bottoms stream.
7) The apparatus of claim 1 , further comprising means for producing the raw synthesis gas by reforming a hydrocarbon, wherein the means for producing the raw synthesis gas comprises autothermal or secondary reforming with excess air.
8) The apparatus of claim 1 , further comprising means for supplying the purified syngas vapor stream to an ammonia synthesis loop to form ammonia.
9) An ammonia process plant comprising:
means for reforming a hydrocarbon to form syngas, wherein the reforming means include an autothermal or secondary reformer and means for supplying excess air to the autothermal or secondary reformer to form a raw syngas stream containing excess nitrogen for ammonia synthesis;
cross-exchanger means for cooling the raw syngas stream;
means for expanding the cooled raw syngas stream from the cross-exchanger;
means for introducing the expanded raw syngas stream to a feed zone in a distillation column;
means for expanding a liquid bottoms stream from the distillation column through a liquid expander with a work output to form a cooled waste fluid stream;
means for rectifying vapor from the feed zone in the distillation column to form an overhead vapor stream of reduced nitrogen and inerts content;
means for cooling the overhead vapor stream in indirect heat exchange with the cooled waste fluid stream to form a partially condensed overhead stream and a partially warmed waste fluid stream;
means for separating the partially condensed overhead stream into a condensate stream and a purified syngas vapor stream of reduced nitrogen and inerts content;
means for refluxing the distillation column with the condensate stream;
means for heating the purified syngas vapor stream in the cross-exchanger;
means for heating the partially warmed waste fluid stream in the cross exchanger;
means for supplying the purified syngas vapor stream from the cross-exchanger to an ammonia synthesis loop.
10) The ammonia process plant of claim 9 , further comprising means for cooling and expanding the raw syngas stream across a Joule-Thompson valve in advance of the introduction to the feed zone.
11) The ammonia process plant of claim 10 , wherein the means for cooling of the raw syngas stream includes cross-exchange against the partially warmed waste fluid stream and against the purified syngas vapor stream.
12) The ammonia process plant of claim 9 , wherein the means for expanding the liquid bottoms stream comprises a hydraulic turbine.
13) The ammonia process plant of claim 9 , wherein the partially warmed waste fluid stream from cooling of the overhead vapor stream consists of a vapor phase.
14) The ammonia process plant of claim 9 , wherein waste fluid from the liquid expander comprises mixed vapor and liquid.
15) The ammonia process plant of claim 9 , wherein a liquid level in the distillation column is controlled by adjusting flow the expansion to the liquid bottoms stream.
16) The ammonia process plant of claim 9 , further comprising means for producing the raw synthesis gas by reforming a hydrocarbon, wherein the means for producing the raw synthesis gas comprises autothermal or secondary reforming with excess air.
17) The ammonia process plant of claim 9 , further comprising means for supplying the purified syngas vapor stream to an ammonia synthesis loop to form ammonia.
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- 2004-07-15 EP EP04016768A patent/EP1503160B1/en active Active
- 2004-07-15 DE DE602004016796T patent/DE602004016796D1/en active Active
- 2004-07-16 RU RU2004121999/15A patent/RU2331575C2/en active
- 2004-07-16 MX MXPA04006957A patent/MXPA04006957A/en active IP Right Grant
- 2004-07-16 CN CNB2004100712290A patent/CN100519406C/en active Active
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US20120308466A1 (en) * | 2007-08-08 | 2012-12-06 | Ammonia Casale S.A. | Process for Producing Ammonia Synthesis Gas |
US20150086465A1 (en) * | 2007-08-08 | 2015-03-26 | Casale Sa | Process for Producing Ammonia Synthesis Gas |
US10464818B2 (en) | 2007-08-08 | 2019-11-05 | Casale Sa | Process for producing ammonia synthesis gas |
US20100051876A1 (en) * | 2008-08-28 | 2010-03-04 | Ammonia Casale S.A. | Process for the production of ammonia synthesis gas with improved cryogenic purification |
US20100300144A1 (en) * | 2009-04-24 | 2010-12-02 | Madison Joel V | Liquefied Gas Expander And Integrated Joule-Thomson Valve |
US8683824B2 (en) * | 2009-04-24 | 2014-04-01 | Ebara International Corporation | Liquefied gas expander and integrated Joule-Thomson valve |
US9335092B2 (en) | 2009-04-24 | 2016-05-10 | Ebara International Corporation | Method of gas expansion using liquefied gas expander and integrated Joule-Thomson valve |
US9593882B2 (en) | 2009-04-24 | 2017-03-14 | Ebara International Corporation | Three-way integrated Joule-Thomson valve and liquefied gas expander |
WO2014207011A1 (en) * | 2013-06-26 | 2014-12-31 | Casale Sa | A process for purification of a synthesis gas containing hydrogen and impurities |
EP2818447A1 (en) * | 2013-06-26 | 2014-12-31 | Ammonia Casale S.A. | A process for purification of a synthesis gas containing hydrogen and impurities |
US10816264B2 (en) | 2013-06-26 | 2020-10-27 | Casale Sa | Process for purification of a synthesis gas containing hydrogen and impurities |
CN109612203A (en) * | 2018-11-22 | 2019-04-12 | 山东润银生物化工股份有限公司 | A kind of processing method of discharge gas in ammonia synthesis |
Also Published As
Publication number | Publication date |
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EP1503160A1 (en) | 2005-02-02 |
RU2004121999A (en) | 2006-01-20 |
CN100519406C (en) | 2009-07-29 |
RU2331575C2 (en) | 2008-08-20 |
CA2473045A1 (en) | 2005-01-17 |
CA2473045C (en) | 2011-09-27 |
DE602004016796D1 (en) | 2008-11-13 |
CN1597496A (en) | 2005-03-23 |
EP1503160B1 (en) | 2008-10-01 |
MXPA04006957A (en) | 2005-06-17 |
US7090816B2 (en) | 2006-08-15 |
US20050013768A1 (en) | 2005-01-20 |
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