Patent Grant
12117240
The following abbreviations are used herein: multicomponent refrigerant (MR), air separation unit (ASU), main air compressor (MAC), booster air compressor (BAC), liquefied natural gas (LNG), oxygen (O2), nitrogen (N2), gaseous oxygen (GOX), liquid oxygen (LOX), liquid nitrogen (LIN), liquid argon (LAR), and liquid air (LAIR).
A simple mass and energy balance around the cold end of an ASU (distillation columns+sub-cooler) indicates that the quantity of liquid leaving must be approximately equal to the quantity of liquid entering. Also, for an efficient distillation it is known in the art that the air entering the bottom of the distillation column should be cold vapor near the dew point. Therefore, a simple energy balance requires that a liquid stream (typically LAIR) enter the columns and has a flowrate approximately equal to the sum of the LOX+LIN products.
Prior art schemes utilize only low-pressure air (4 to 7 bara) from the main air compressor to distillation column. Per the above cold end energy balance, liquid air must be leaving cold end of main exchanger and entering the distillation. Condensing at such low pressure (4 to 7 bara is significantly below the critical pressure of 62 bara) yields very high latent heat of condensation. As the flowrate of the liquid air increases (due to increasing flowrate of LOX+LIN), the heat exchange to produce this LAIR becomes infeasible without vaporizing another stream in the main exchanger to provide additional refrigeration. This is the case particularly when significant quantities of O2 are removed from the process as liquid (LOX) rather than being pumped to higher pressure and vaporized in the main exchanger against the condensing air stream producing high pressure GOX. Note that the flow of vaporizing MR is already compensated by the condensing of the MR.
In the current application significant quantities of O2 are removed as LOX rather than vaporizing to produce High Pressure GOX such that at least 80% of oxygen in feed air is produced as liquid oxygen. Or the mass flow of LOX+LIN is greater than mass flow of oxygen in feed air.
Referring now to
Oxygen-enriched liquid is withdrawn from the lower portion of higher-pressure column 103 in stream 110 and passed to sub-cooler 111 wherein it is subcooled. Resulting subcooled oxygen-enriched liquid is then divided into first portion 112 and second portion 113. First portion 112 is passed into lower pressure column 108 and second portion 113 is passed into argon column condenser 114 wherein it is at least partially vaporized. The resulting vapor is withdrawn from condenser 114 and passed into lower pressure column 108. Any remaining oxygen-enriched liquid is withdrawn from condenser 114 and then passed into lower pressure column 108.
Lower pressure column 108 is operating at a pressure less than that of higher-pressure column 103 and generally within the range of from 15 to 150 psia. Within lower pressure column 108 the various feeds into that column are separated by cryogenic rectification into nitrogen-rich vapor and oxygen-rich liquid. Nitrogen-rich vapor is withdrawn from the upper portion of lower pressure column 108 in stream 115, warmed by passage through heat exchangers 103, 111, and 107, and may be recovered as product gaseous nitrogen having a nitrogen concentration of at least 99 mole percent, preferably at least 99.9 mole percent, and most preferably at least 99.999 mole percent. For product purity control purposes, a waste stream 116 is withdrawn from lower pressure column 108 from a level below the withdrawal point of stream 115, warmed by passage through heat exchangers 103, 111, and 107, and removed from the system. Oxygen-rich liquid is partially vaporized in the lower portion of lower pressure column 108 by indirect heat exchange with condensing nitrogen-enriched vapor in main condenser 105 as was previously described to provide vapor up-flow for lower pressure column 108. If desired, a portion of the resulting oxygen-rich vapor may be withdrawn from the lower portion of lower pressure column 108 in stream 118 having an oxygen concentration generally within the range of from 90 to 99.9 mole percent. Oxygen-rich vapor in stream 118 is warmed by passage through main heat exchanger 102 and recovered as product gaseous oxygen in stream 119. Oxygen-rich liquid is withdrawn from the lower portion of lower pressure column 108 in stream 120 and recovered as liquid oxygen. Stream 120 may comprise all of the oxygen contained in the feed air.
Fluid comprising oxygen and argon is passed in stream 121 from lower pressure column 108 into third or argon column 122 wherein it is separated by cryogenic rectification into argon-richer fluid and oxygen-richer fluid. Oxygen-richer fluid is passed from the lower portion of column 122 in stream 123 into lower pressure column 108. Argon-richer fluid is passed from the upper portion of column 122 as vapor into argon column condenser 114 wherein it is condensed by indirect heat exchange with the aforesaid subcooled oxygen-enriched liquid. Resulting argon-richer liquid is withdrawn from condenser 114. At least a portion of the argon-richer liquid is passed into argon column 122 as reflux and, if desired, another portion is recovered as product liquid argon as shown by stream 124. Stream 124 may comprise all of the argon in the feed air.
There will now be described in greater detail the operation of the multicomponent refrigerant fluid circuit which serves to generate preferably all the refrigeration passed into the cryogenic rectification plant thereby eliminating the need for any turbo-expansion of a process stream to produce refrigeration for the separation, thus decoupling the generation of refrigeration for the cryogenic air separation process from the flow of process streams, such as feed air, associated with the cryogenic air separation process. It should be understood that this is simply one example of a multicomponent refrigerant system, and any alternative system that is known in the art that is suitable for this application may be substituted by one skilled in the art.
The following description illustrates the multicomponent refrigerant fluid system for providing refrigeration throughout the main heat exchanger 102. Multicomponent refrigerant fluid in stream 125 is compressed by passage through recycle compressor 126 to a pressure generally within the range of from 45 to 81400 psia to produce a compressed refrigerant fluid. The compressed refrigerant fluid is cooled of the heat of compression by passage through aftercooler 127 and may be partially condensed. The resulting multicomponent refrigerant fluid 128 is then passed through main heat exchanger 102 wherein it is further cooled and generally is at least partially condensed and may be completely condensed. The resulting cooled, compressed multicomponent refrigerant fluid 129 is then expanded or throttled through valve 130. The throttling preferably partially vaporizes the multicomponent refrigerant fluid, cooling the fluid and generating refrigeration. For some limited circumstances, dependent on heat exchanger conditions, the compressed fluid 129 may be subcooled liquid prior to expansion and may remain as liquid upon initial expansion. Subsequently, upon warming in the heat exchanger, the fluid will have two phases. The pressure expansion of the fluid through a valve would provide refrigeration by the Joule-Thomson effect, i.e. lowering of the fluid temperature due to pressure expansion at constant enthalpy. However, under some circumstances, the fluid expansion could occur by utilizing a two-phase or liquid expansion turbine, so that the fluid temperature would be lowered due to work expansion.
Refrigeration bearing multicomponent two phase refrigerant fluid stream 131 is then passed through main heat exchanger 102 wherein it is warmed and completely vaporized thus serving by indirect heat exchange to cool stream 128 and also to transfer refrigeration into the process streams within the heat exchanger, including feed air stream 101, thus passing refrigeration generated by the multicomponent refrigerant fluid refrigeration circuit into the cryogenic rectification plant to sustain the cryogenic air separation process. The resulting warmed multicomponent refrigerant fluid in vapor stream 125 is then recycled to compressor 126 and the refrigeration cycle starts anew. In the multicomponent refrigerant fluid refrigeration cycle while the high-pressure mixture is condensing, the low-pressure mixture is boiling against it, i.e. the heat of condensation boils the low-pressure liquid. At each temperature level, the net difference between the vaporization and the condensation provides the refrigeration. For a given refrigerant component combination, mixture composition, flowrate and pressure levels determine the available refrigeration at each temperature level.
The multicomponent refrigerant fluid contains two or more components in order to provide the required refrigeration at each temperature. The choice of refrigerant components will depend on the refrigeration load versus temperature for the specific process. Suitable components will be chosen depending upon their normal boiling points, latent heat, and flammability, toxicity, and ozone-depletion potential.
Alternatively, this cold end refrigeration balance can be managed by LIN assist from an external liquefier. In this case the flowrate of LIN assist is approximately equal to the flow rate of LOX production, as described below in
Turning now to
After passing through liquefaction heat exchanger 209, first vapor portion 207 exits as warmed first vapor stream 242. Warmed first vapor stream 242 is introduced to second phase separator vessel 243, which produces second vapor portion 244 and second liquid portion 245. Second vapor portion 244 is introduced into liquefaction heat exchanger 411. After passing through liquefaction heat exchanger 209 second vapor portion 244 exits as cooled to form at least partially condensed portion 246. Second liquid portion 245 is introduced into liquefaction heat exchanger 209. After passing through liquefaction heat exchanger 209, second liquid portion 245 exits as warm second liquid portion 247.
After passing through liquefaction heat exchanger 209, first liquid portion 208 exits as warmed first liquid stream 248. At least partially condensed portion 246 is introduced into third phase separator vessel 249. Third phase separator vessel 249 produces third vapor portion 250 and third liquid portion 251. Third vapor portion 250 and third liquid portion 251 are combined to form third combined multicomponent refrigerant stream 252, which is introduced into liquefaction heat exchanger 209. After passing through liquefaction heat exchanger 209, third combined multicomponent refrigerant stream 252 exits as warm combined multicomponent refrigerant steam 253.
Warmed second liquid portion 247 is introduced into fourth phase separator vessel 254. Warmed first liquid stream 248 is introduced into fourth phase separator vessel 254. And warm combined nitrogen steam 253 are introduced to fourth phase separator vessel 254. Exiting fourth phase separator vessel 254 are fourth vapor portion 255 and fourth liquid portion 256. Fourth vapor portion 255 and fourth liquid portion 256 are combined to form fourth combined multicomponent refrigerant stream 257, which is introduced into liquefaction heat exchanger 209. After passing through liquefaction heat exchanger 209, fourth combined multicomponent refrigerant stream 257 exits as warm multicomponent refrigerant return steam 201.
It is understood, but not shown in
Nitrogen refrigeration cycle includes increasing the pressure of first nitrogen recycle stream 210 in LP nitrogen compressor 211, thereby producing warm medium-pressure nitrogen stream 212. Warm medium-pressure nitrogen stream 212 enters first nitrogen cooler 213, thereby producing cooled medium-pressure nitrogen stream 214.
Cooled medium-pressure nitrogen stream 214 is combined with medium-pressure nitrogen stream 240 from ASU 215 and second nitrogen recycle stream 216, thereby producing combined medium-pressure nitrogen stream 217. The pressure of medium-pressure nitrogen stream 217 is increased in MP nitrogen compressor 218, thereby producing warm intermediate-pressure nitrogen stream 219. Warm intermediate-pressure nitrogen stream 219 enters second nitrogen cooler 220, thereby producing cooled intermediate-pressure nitrogen stream 221.
Cooled intermediate-pressure nitrogen stream 221 is then further compressed in HP nitrogen booster 222, thereby producing high-pressure nitrogen stream 223. High-pressure nitrogen stream 223 then passes through liquefaction heat exchanger 209, after which it is removed at two locations. Typically, first nitrogen refrigeration stream 224 will be removed as a vapor stream, and second nitrogen refrigeration stream 225 will be removed as a liquid stream.
The first location is via first nitrogen refrigeration stream 224, which is then introduced into nitrogen expander 226. Nitrogen expander 276 is connected to HP nitrogen booster 273 by a common drive shaft. After having the pressure reduced in nitrogen expander 276, this stream exits as expanded nitrogen stream 227, which is then introduced into liquefaction heat exchanger 411. Expanded nitrogen stream 227 exits liquefaction heat exchanger 209 as second nitrogen recycle stream 216.
The second location is via second nitrogen refrigeration stream 225, which is then introduced third phase separator vessel 228, which produces nitrogen vapor portion 229 and nitrogen liquid portion 230. Nitrogen vapor portion 229 and nitrogen liquid portion 230 are combined to form combined nitrogen stream 231. A portion of combined nitrogen stream 231 is removed as internal liquid nitrogen stream 232. At least a portion 233 of internal liquid nitrogen stream 232 is returned to the ASU, and a portion of internal liquid nitrogen stream 232 may be removed as external LIN product to storage 234. The remaining portion of combined nitrogen stream 231 is introduced into liquefaction heat exchanger 209 as cold nitrogen recycle stream 235. Cold nitrogen recycle stream 235 exits liquefaction heat exchanger 209 as first nitrogen recycle stream 210.
Multicomponent refrigerant cycle and nitrogen refrigeration cycle work together to provide sufficient refrigeration duty to liquefy inlet natural gas stream 236 into liquid natural gas stream 237. In addition, these combined refrigeration streams also provide sufficient additional refrigeration duty via internal liquid nitrogen stream 233, to satisfy the duty requirements of air separation unit 215.
Compressed and purified inlet air stream 238 enters first heat exchanger 239 wherein it exchanges heat with medium-pressure nitrogen stream 240, then enters air separation unit 215. Air separation unit 215 produces at least medium-pressure nitrogen stream 240, and liquid oxygen stream 241. In order to produce the desired flowrate in liquid oxygen stream 241, it is necessary to introduce additional refrigeration duty, in the form of internal liquid nitrogen stream 233.
Medium-pressure nitrogen stream 240 and inlet natural gas stream 236 are introduced into liquefaction heat exchanger 209, as described above. Liquefaction heat exchanger 209 outputs at least liquid natural gas stream 237 and internal liquid nitrogen stream 232. Liquid natural gas stream 237 is then sent to liquid natural gas storage.
To avoid the excessive energy associated with the sensible heat of rewarming and cooling the N2 feed stream t the liquefier, it could be envisioned to send the cold gaseous N2 directly from the MP column to a cold location in the liquefier. (not warming the gaseous N2 in the ASU). However, in this case the ASU main exchanger heat transfer is imbalanced as the flow of the streams is much higher than the flow of cold streams resulting in unparalleled heat exchange lines as indicated in
Note, that in
A process for the production of a liquid oxygen stream by the cryogenic rectification of an inlet air stream, including dividing the inlet air stream into a first portion, and a second portion. Cooling the first portion, and the second portion against a cooled multicomponent refrigerant circuit, thereby producing a first cooled portion, and a second cooled portion. The multicomponent refrigerant circuit including compressing a multicomponent refrigerant stream, thereby producing a pressurized multicomponent refrigerant stream, cooling the pressurized multicomponent refrigerant stream, thereby producing a cooled multicomponent refrigerant stream, expanding the cooled multicomponent refrigerant stream, thereby producing an expanded multicomponent refrigerant stream, and warming the expanded multicomponent refrigerant stream by indirect heat exchange with the compressed multicomponent refrigerant stream and with the first portion, and the second portion Condensing the first cooled portion, thereby producing a condensed first portion, then introducing the condensed first portion into one or more distillation columns. Expanding the second cooled portion in a turbo-expander, thereby producing an expanded second portion, then introducing the expanded second portion within the one or more distillation columns. Producing within the one or more distillation columns at least a waste nitrogen stream, a nitrogen enriched stream, and an oxygen enriched stream. Withdrawing the oxygen enriched stream from the one or more distillation columns as a liquid oxygen stream.
A process for the production of a liquid oxygen stream by the cryogenic rectification of an inlet air stream, including dividing the inlet air stream into a first portion, a second portion, and a third portion. Cooling the first portion, the second portion, and the third portion against a cooled multicomponent refrigerant circuit, thereby producing a first cooled portion, a second cooled portion, and a third cooled portion. The multicomponent refrigerant circuit including compressing a multicomponent refrigerant stream, thereby producing a compressed multicomponent refrigerant stream. Cooling the compressed multicomponent refrigerant stream, thereby producing a cooled multicomponent refrigerant stream. Expanding the cooled multicomponent refrigerant stream, thereby producing an expanded multicomponent refrigerant stream. And warming the expanded multicomponent refrigerant stream by indirect heat exchange with the compressed multicomponent refrigerant stream and with the first portion, the second portion, and the third portion. Condensing the first cooled portion, thereby producing a condensed first portion, then introducing the expanded first portion into one or more distillation columns. Expanding the second cooled portion in a turbo-expander, thereby producing an expanded second portion, then introducing the expanded second portion into the one or more distillation columns. Introducing the third cooled portion into one or more distillation columns. Producing within the one or more distillation columns at least a nitrogen enriched stream and an oxygen enriched stream. Withdrawing the oxygen enriched stream from the one or more distillation columns as a liquid oxygen stream.
A process for the production of liquid oxygen by the cryogenic rectification of an inlet air stream, including compressing the inlet air stream in a main air compressor to a pressure greater than 10 bara, thereby producing a compressed inlet air stream. Removing water and carbon dioxide from the compressed inlet air stream, thereby forming a purified inlet air stream. Boosting the purified inlet air stream in a booster driven by a turbo-expander, thereby producing a boosted inlet air stream. Cooling the boosted inlet air stream, thereby producing a cooled boosted inlet air stream. Splitting the cooled boosted inlet air stream into a first boosted inlet air stream and a second boosted air stream. Liquefying the first boosted inlet air stream, thereby producing a liquefied inlet air stream, which is then introduced into the distillation column. Expanding the second boosted air stream in one or more turbo-expanders, thereby producing an expanded air stream, which is then introduced into a distillation column. And compressing a multicomponent refrigerant stream, thereby producing a compressed multicomponent refrigerant stream. Cooling the compressed multicomponent refrigerant fluid, thereby producing a cooled multicomponent refrigerant stream. Expanding the cooled multicomponent refrigerant stream, thereby producing an expanded multicomponent refrigerant stream. And warming the expanded multicomponent refrigerant stream by indirect heat exchange with the compressed multicomponent refrigerant stream and with the boosted inlet air stream to produce the cooled boosted inlet air stream. And producing in the one or more distillation columns a nitrogen enriched stream and an oxygen enriched stream. And withdrawing the oxygen enriched stream from the one or more distillation columns as a liquid oxygen stream.
A process for the production of liquid oxygen by the cryogenic rectification of an inlet air stream, including compressing the inlet air stream in a main air compressor to a pressure greater than 20 bara, thereby producing a compressed inlet air stream. Removing water and carbon dioxide from the compressed inlet air stream, thereby forming a purified inlet air stream. Splitting the purified feed stream into a first fraction and a second fraction. Cooling the first fraction, thereby producing a cooled first fraction, which is then introduced into a distillation column. Boosting the second fraction in a booster driven by a turbo-expander, thereby producing a boosted inlet air stream. Cooling the boosted inlet air stream, thereby producing a cooled boosted inlet air stream. Splitting the cooled boosted inlet air stream into a first boosted inlet air stream and a second boosted air stream. Liquefying the first boosted inlet air stream, thereby producing a liquefied inlet air stream, which is then introduced into the distillation column. Expanding the second boosted air stream in one or more turbo-expanders, thereby producing an expanded air stream, which is then introduced into the distillation column. Compressing a multicomponent refrigerant stream, thereby producing a compressed multicomponent refrigerant stream. Cooling the compressed multicomponent refrigerant fluid, thereby producing a cooled multicomponent refrigerant stream. Expanding the cooled multicomponent refrigerant stream, thereby producing an expanded multicomponent refrigerant stream. Warming the expanded multicomponent refrigerant stream by indirect heat exchange with the compressed multicomponent refrigerant stream and with the boosted inlet air stream to produce the cooled boosted inlet air stream. Producing in the one or more distillation columns a nitrogen enriched stream and an oxygen enriched stream. And withdrawing the oxygen enriched stream from the one or more distillation columns as a liquid oxygen stream.
For a further understanding of the nature and objects for the present invention, reference should be made to the following detailed description, taken in conjunction with the accompanying drawings, in which like elements are given the same or analogous reference numbers and wherein:
Illustrative embodiments of the invention are described below. While the invention is susceptible to various modifications and alternative forms, specific embodiments thereof have been shown by way of example in the drawings and are herein described in detail. It should be understood, however, that the description herein of specific embodiments is not intended to limit the invention to the particular forms disclosed, but on the contrary, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the invention as defined by the appended claims.
It will of course be appreciated that in the development of any such actual embodiment, numerous implementation-specific decisions must be made to achieve the developer's specific goals, such as compliance with system-related and business-related constraints, which will vary from one implementation to another. Moreover, it will be appreciated that such a development effort might be complex and time-consuming, but would nevertheless be a routine undertaking for those of ordinary skill in the art having the benefit of this disclosure.
Using Claude Turbine Booster (Claude compressor 327 and Claude expander 333) with a condensing air stream at the cold section of main exchanger combined with a multicomponent refrigerant cycle for the warm section of the main exchanger. The MAC outlet is ˜30 to 35 bara and the outlet of the booster is 35 to 45 bara such that the condensing air stream is 34 to 45 bara resulting in low latent heat of condensation.
Prior art integration of MR cycle with an ASU produces at least some oxygen which enters the main heat exchanger for indirect heat exchange with the multicomponent refrigerant fluid. The current application does not have any oxygen enriched stream in main heat exchanger. Nothing greater than air, 21% O2. This provides safer management of flammable multicomponent refrigerants than prior art.
Turning now to
After passing through liquefaction heat exchanger 347, first vapor portion 309 exits as warmed first vapor stream 311. Warmed first vapor stream 311 is introduced to second phase separator vessel 312, which produces second vapor portion 313 and second liquid portion 314. Second vapor portion 313 and second liquid portion 314 are combined to form second combined multicomponent refrigerant stream 315, which is introduced into liquefaction heat exchanger 347. After passing through liquefaction heat exchanger 347 second combined multicomponent refrigerant stream 315 exits as warmed combined nitrogen stream 316.
After passing through liquefaction heat exchanger 347, first liquid portion 310 exits as warmed first liquid stream 317. Warmed first liquid stream 317 and warmed combined nitrogen stream 316 are introduced into third phase separator vessel 318. Third phase separator vessel 318 produces third vapor portion 319 and third liquid portion 320. Third vapor portion 319 and third liquid portion 320 are combined to form third combined multicomponent refrigerant stream 321, which is introduced into liquefaction heat exchanger 347. After passing through liquefaction heat exchanger 347, third combined multicomponent refrigerant stream 321 exits as warm multicomponent refrigerant return steam 301.
Multicomponent refrigerant cycle and nitrogen refrigeration cycle work together to provide sufficient refrigeration duty to liquefy inlet natural gas stream 236 into liquid natural gas stream 237. In addition, these combined refrigeration streams also provide sufficient additional refrigeration duty via internal liquid nitrogen stream 233, to satisfy the duty requirements of air separation unit 215.
Inlet air stream 322 enters main air compressor 323 wherein the pressure is increased, and the pressurized air is cooled in inlet air cooler 324. The cooled, compressed air stream is then directed to one of air purification vessel 325a/b, wherein the inlet air stream is purified, thereby producing purified inlet air stream 326. Purified inlet air stream 325 is then compressed in Claude compressor 327 and cooled in boosted air cooler 328. Cooled, boosted air stream 329 then enters liquefaction heat exchanger 347, thereby forming cold air stream 330. After having the temperature reduced, first portion 331 of cold air stream 330 exits liquefaction heat exchanger 347 and then enters distillation column 335. Second portion 332 of the cold air stream 330 continues through liquefaction heat exchanger 347 and exits liquefaction heat exchanger 347 and then enters Claude expander 333. Expanded second air stream 334 then enters Claude expander 333. Distillation column 335 produces at least liquid nitrogen product stream 336, waste nitrogen stream 342, liquid oxygen stream 338, and liquid oxygen product stream 337. In order to produce the desired flowrate in both liquid oxygen stream 338 and liquid oxygen product stream 337, it is necessary to introduce additional refrigeration duty, in the form of expanded second air stream 334. At least a portion of the liquid oxygen from distillation column 335 may be exported as a liquid oxygen product stream 337.
Optionally, liquid oxygen stream 338 may be removed from distillation column 335. Liquid oxygen stream 338 is increased in pressure in liquid oxygen pump 339, thereby producing high-pressure liquid oxygen stream 340. High-pressure liquid oxygen stream 340 is then introduced into liquefaction heat exchanger 347, wherein it is heated and vaporized, thereby producing optional high-pressure gaseous oxygen product stream 341, which then exits the system. One skilled in the art will recognize that liquid oxygen pump 339 may just as easily product low-pressure or medium-pressure liquid oxygen, and therefore the system may produce low-pressure or medium-pressure gaseous oxygen (not shown) in addition to the high-pressure gaseous oxygen system as illustrated. All oxygen product streams may be only liquid. Or a portion may be liquid and additional (optional) portions maybe low-pressure gaseous oxygen and/or high-pressure gaseous oxygen.
After passing through liquefaction heat exchanger 347, warmed waste nitrogen stream 353 is heated in waste nitrogen heater 354, thereby producing hot waste nitrogen stream 355. Hot waste nitrogen stream 355 is then used to regenerate air purification vessels 325a/b as needed, with the resulting regeneration waste exiting in regeneration waste streams 356a/b.
In this case the ASU main exchanger heat transfer is balanced, as indicated in the parallel heat exchange lines as indicated in
In an alternative embodiment, as illustrated in
Turning now to
After passing through liquefaction heat exchanger 347, first vapor portion 309 exits as warmed first vapor stream 311. Warmed first vapor stream 311 is introduced to second phase separator vessel 312, which produces second vapor portion 313 and second liquid portion 314. Second vapor portion 313 and second liquid portion 314 are combined to form second combined multicomponent refrigerant stream 315, which is introduced into liquefaction heat exchanger 347. After passing through liquefaction heat exchanger 347 second combined multicomponent refrigerant stream 315 exits as warmed combined nitrogen stream 316.
After passing through liquefaction heat exchanger 347, first liquid portion 310 exits as warmed first liquid stream 317. Warmed first liquid stream 317 and warmed combined nitrogen stream 316 are introduced into third phase separator vessel 318. Third phase separator vessel 318 produces third vapor portion 319 and third liquid portion 320. Third vapor portion 319 and third liquid portion 320 are combined to form third combined multicomponent refrigerant stream 321, which is introduced into liquefaction heat exchanger 347. After passing through liquefaction heat exchanger 347, third combined multicomponent refrigerant stream 321 exits as warm multicomponent refrigerant return steam 301.
Multicomponent refrigerant cycle and nitrogen refrigeration cycle work together to provide sufficient refrigeration duty to liquefy inlet natural gas stream 236 into liquid natural gas stream 237. In addition, these combined refrigeration streams also provide sufficient additional refrigeration duty via internal liquid nitrogen stream 233, to satisfy the duty requirements of air separation unit 215.
Inlet air stream 322 enters main air compressor 323 wherein the pressure is increased, and the pressurized air is cooled in inlet air cooler 324. The cooled, compressed air stream is then directed to one of air purification vessel 325a/b, wherein the inlet air stream is purified, thereby producing purified inlet air stream 325. Purified air stream 325 is split into two portions.
First portion 601 enters liquefaction heat exchanger 347 and exits as cooled feed stream 602, which then enters distillation column 335. Second portion 603 enters booster air compressor 604, thereby producing pressurized first portion 605. Pressurized first portion 605 is then compressed in Claude compressor 327 and cooled in boosted air cooler 328, after which it enters liquefaction heat exchanger 347. First portion 331 of the cooled inlet air exits liquefaction heat exchanger 347 and then enters distillation column 335. Second portion 332 of the cooled inlet air exits liquefaction heat exchanger 347 and then enters Claude expander 333. Expanded second air stream 334 then enters Claude expander 333. Distillation column 335 produces at least liquid nitrogen product stream 336, waste nitrogen stream 342, and liquid oxygen product stream 337. In order to produce the desired flowrate in liquid oxygen product stream 337, it is necessary to introduce additional refrigeration duty, in the form of expanded second air stream 334. At least a portion of the liquid oxygen from distillation column 335 may be exported as a liquid oxygen product stream 337.
Optionally, liquid oxygen stream 338 may be removed from distillation column 335. Liquid oxygen stream 338 is increased in pressure in liquid oxygen pump 339, thereby producing high-pressure liquid oxygen stream 340. High-pressure liquid oxygen stream 340 is then introduced into liquefaction heat exchanger 347, wherein it is heated and vaporized, thereby producing optional high-pressure gaseous oxygen product stream 341, which then exits the system. One skilled in the art will recognize that liquid oxygen pump 339 may just as easily product low-pressure or medium-pressure liquid oxygen, and therefore the system may produce low-pressure or medium-pressure gaseous oxygen (not shown) in addition to the high-pressure gaseous oxygen system as illustrated. All oxygen product streams may be only liquid. Or a portion may be liquid and additional (optional) portions maybe low-pressure gaseous oxygen and/or high-pressure gaseous oxygen.
After waste nitrogen stream 342 passes through liquefaction heat exchanger 347, warmed waste nitrogen stream 343 is heated in waste nitrogen heater 344, thereby producing hot waste nitrogen stream 345. Hot waste nitrogen stream 345 is then used to regenerate air purification vessels 346a/b as needed, with the resulting regeneration.
It will be understood that many additional changes in the details, materials, steps and arrangement of parts, which have been herein described in order to explain the nature of the invention, may be made by those skilled in the art within the principle and scope of the invention as expressed in the appended claims. Thus, the present invention is not intended to be limited to the specific embodiments in the examples given above.
This application claims the benefit of priority under 35 U.S.C. § 119 (a) and (b) to U.S. Provisional Patent Application No. 63/223,410, filed Jul. 19, 2021, the entire contents of which are incorporated herein by reference.
| Number | Name | Date | Kind |
|---|---|---|---|
| 4375367 | Prentice | Mar 1983 | A |
| 6053008 | Arman et al. | Apr 2000 | A |
| 6112550 | Bonaquist et al. | Sep 2000 | A |
| 6230519 | Arman et al. | May 2001 | B1 |
| 6253577 | Arman et al. | Jul 2001 | B1 |
| 6260380 | Arman et al. | Jul 2001 | B1 |
| 9671160 | Wyllie | Jun 2017 | B2 |
| 10662821 | Castellucci | May 2020 | B2 |
| 10866022 | Krishnamurthy | Dec 2020 | B2 |
| 20110100055 | Brigham | May 2011 | A1 |
| 20110203312 | Jakobsen et al. | Aug 2011 | A1 |
| 20130068220 | Kudaravalli | Mar 2013 | A1 |
| 20140109386 | Matthews | Apr 2014 | A1 |
| 20150345857 | Rauch | Dec 2015 | A1 |
| 20170038136 | Turney et al. | Feb 2017 | A1 |
| 20170038138 | Turney | Feb 2017 | A1 |
| 20170299261 | Narinsky | Oct 2017 | A1 |
| 20190135626 | Rafati | May 2019 | A1 |
| Number | Date | Country | |
|---|---|---|---|
| 20230018749 A1 | Jan 2023 | US |
| Number | Date | Country | |
|---|---|---|---|
| 63223410 | Jul 2021 | US |
