US20130118204A1 - Integrated liquid storage - Google Patents

Integrated liquid storage Download PDF

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Publication number
US20130118204A1
US20130118204A1 US13/811,703 US201013811703A US2013118204A1 US 20130118204 A1 US20130118204 A1 US 20130118204A1 US 201013811703 A US201013811703 A US 201013811703A US 2013118204 A1 US2013118204 A1 US 2013118204A1
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United States
Prior art keywords
stream
pressure
storage tank
phase
high pressure
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US13/811,703
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English (en)
Inventor
Paul Higginbotham
Anthony Knut James Topham
Kevin David Thomas Tapsfield
John Crawford Rossman
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Air Products and Chemicals Inc
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Air Products and Chemicals Inc
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Assigned to AIR PRODUCTS AND CHEMICALS, INC. reassignment AIR PRODUCTS AND CHEMICALS, INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: ROSSMAN, JOHN CRAWFORD, HIGGINBOTHAM, PAUL, TAPSFIELD, KEVIN DAVID THOMAS, TOPHAM, ANTHONY KNUT JAMES
Publication of US20130118204A1 publication Critical patent/US20130118204A1/en
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    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
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    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/34—Details about subcooling of liquids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • Nitrogen liquefiers are well known in the art and are generally linked to a nitrogen generator, for example, or an Air Separation Unit (ASU). Liquefiers may be used to liquefy low pressure gaseous nitrogen from an ASU, for example. Liquefiers may also take at least a part of their feed from the ASU at higher pressure and/or at cryogenic temperatures for liquefying purposes.
  • ASU Air Separation Unit
  • This subcooling may take place by pressure reduction in a second separator at a lower pressure or indirectly in a subcooler by heat exchange against a boiling liquid at low pressure.
  • the use of a subcooler allows enough pressure to be maintained in the liquid to transfer it to storage without using pumps, for example.
  • Portions of the liquid produced in the liquefier may be stored, for example, in an insulated liquid storage tank for future use or be exported by road tanker while other portions of the liquid may be returned to the ASU to provide refrigeration, for example.
  • the second separator must be elevated above the level of the storage tank if the use of additional pumps is to be avoided.
  • the described embodiments satisfy the need in the art by providing a simplified and efficient liquefier using a liquid storage tank as a flash separator and recovering the flash and boil-off vapor from storage through the liquefier. Separators and subcoolers may be eliminated from the liquefier design and process. As the cold portion of the liquefier is essentially only a heat exchanger and piping, it may be insulated directly and the separate cold box structure eliminated.
  • the described embodiments utilize a design and process that is opposed to conventional wisdom for the construction of efficient liquefier designs and processes.
  • Production of liquid in a separate liquefier rather than in an ASU plant has operational advantages such as being easy to turn on and off according to demand, but has the significant disadvantages of the high capital cost and lower efficiency associated with a separate process unit.
  • increasing process efficiency will increase capital cost, and capital cost has to be increased to improve efficiency.
  • the process and system described allows this capital cost to be reduced at the same time as improving the efficiency.
  • a process for liquefying a gas comprising introducing a feed stream into a liquefier comprising at least a warm expander and a cold expander; compressing the feed stream in the liquefier to a pressure greater than its critical pressure and cooling the compressed feed stream to a temperature below its critical temperature to form a high pressure dense-phase stream; removing the high pressure dense-phase stream from the liquefier and reducing the pressure of the high pressure dense-phase stream in an expansion device to form a resultant two-phase stream and then directly introducing the resultant two-phase stream into a storage tank; and combining a flash portion of the resultant two-phase stream with a boil-off vapor from a liquid in the storage tank to form a combined vapor stream, wherein the temperature of the high pressure dense-phase stream is lower than the temperature of a discharge stream of the cold expander.
  • a system for liquefying an atmospheric gas comprising: a first conduit for accepting a feed stream; a liquefier fluidly connected to the first conduit for compressing and cooling the feed stream to form a high pressure dense phase fluid, wherein the liquefier comprises at least a warm expander, a cold expander, a compressor for compressing the feed stream to a pressure greater than its critical pressure, and a heat exchanger, for cooling the compressed feed stream to a temperature below its critical temperature; a second conduit fluidly connected to the liquefier for accepting the high pressure dense-phase stream from the liquefier; a first expansion device fluidly connected to the second conduit to reduce the pressure of the high pressure dense-phase stream to form a resultant two-phase stream; a third conduit fluidly connected to the first expansion device for accepting the two-phase expanded stream; and a storage tank fluidly connected to the third conduit for accepting and storing the two-phase expanded stream, wherein the storage tank is designed to operate at a pressure at or below 1.5 bara,
  • FIG. 1 is a flow diagram of an exemplary process for using a liquid storage tank as a flash separator and recovering the flash and boil-off vapor from storage through the liquefier, in accordance with the present invention
  • FIG. 2 is a flow diagram of an alternative exemplary process incorporating a different liquefier configuration
  • FIG. 3 is a flow diagram of a previously disclosed process with the same expander configuration as shown in FIG. 1 , wherein the process includes a cold end separator and subcooler, but comprises no flash vapor or boil-off recovery from the tank; and
  • FIG. 4 is a flow diagram illustrating various ways to integrate the exemplary process of FIG. 1 with an Air Separation Unit where any other process according to the invention may be integrated with the Air Separation Unit in a similar fashion.
  • FIG. 1 illustrates an exemplary system and process for using a liquid storage tank 170 as a flash separator and recovering the flash and boil-off vapor from the liquid storage tank 170 through the liquefier 101 .
  • FIG. 1 discloses low pressure nitrogen feed stream 100 being combined with warmed tank flash and boil-off vapor stream 102 to form combined stream 104 .
  • the low pressure feed stream 100 may be nitrogen, or it may be another gas or gas mixture such as air, oxygen, argon, carbon monoxide, neon, ethylene, helium, or hydrogen, for example.
  • the combined stream 104 is then compressed in the feed compressor 106 to about 6 bara to form compressed stream 108 .
  • Compressed stream 108 is then cooled in an aftercooler 110 to form cooled stream 112 .
  • Cooled stream 112 is then combined with recycle stream 114 to form stream 116 .
  • Stream 116 is then compressed in recycle compressor 118 to about 32 bara resulting in compressed stream 120 .
  • Stream 120 is then cooled in an aftercooler 122 to form stream 124 .
  • Stream 124 is then split into streams 126 and 128 .
  • Stream 126 is (optionally) cooled in the heat exchanger 130 to form stream 132 .
  • Stream 132 is then expanded in warm expander 134 to around 6 bara to form warm expanded stream 136 .
  • Stream 128 is further compressed in the warm compander compressor 138 to form stream 140 .
  • Stream 140 is then cooled in the warm compander aftercooler 142 to form cooled stream 144 .
  • Cooled stream 144 is then compressed again in cold compander compressor 146 to about 65 bara to form compressed stream 148 .
  • Compressed stream 148 is then cooled again in the cold compander compressor aftercooler 150 to form high pressure stream 152 .
  • This high pressure stream 152 is cooled in the heat exchanger 130 to an intermediate temperature of about 182 K, producing streams 154 and 156 .
  • Stream 156 is expanded in a cold expander 158 to form discharge stream 160 .
  • Discharge stream 160 is returned to the cold end of the heat exchanger 130 where it is warmed and mixed with the exhaust stream 136 from the warm expander 134 to form stream 162 .
  • Stream 162 is warmed in heat exchanger 130 to form recycle stream 114 .
  • Recycle stream 114 is then mixed with compressed feed stream 112 and fed to the suction of the recycle compressor 118 .
  • Stream 154 is further cooled in the heat exchanger 130 to form a high pressure dense-phase stream 164 .
  • High pressure dense-phase stream 164 is withdrawn from the cold end of the heat exchanger 130 at a temperature of about 96 K, reduced in pressure across one or more expansion devices 166 to form stream 168 , where stream 168 is fed directly into a liquid storage tank 170 .
  • the term “fed directly” shall mean that the designated stream, after exiting the one or more expansion devices 166 is provided to the liquid storage tank 170 via a conduit without encountering any further apparatus that would alter the composition, temperature, or pressure of the designated stream.
  • directly connected shall mean that a first device or piece of an apparatus is connected to a second device or piece of an apparatus without any intermediate devices or pieces of apparatus that would alter the composition, temperature, or pressure of a stream passing through, for example, the first device to the second device.
  • Stream 168 is flashed into the liquid storage tank 170 to produce mostly liquid with some vapor.
  • the liquid from stream 168 will add to the liquid already present in the liquid storage tank 170 , whilst the flash vapor will combine with boil-off vapor already present in the liquid storage tank 170 .
  • a combined vapor stream 172 composed of flash vapor and boil-off vapor is withdrawn from the liquid storage tank 170 , and, during normal operation, is fed to the heat exchanger 130 of the liquefier 101 as stream 174 .
  • Stream 174 is warmed in the heat exchanger 130 to form warmed tank flash and boil-off vapor stream 102 and mixed with the low pressure feed 100 to form combined stream 104 entering the make-up compressor 106 of the liquefier 101 .
  • the liquid storage tank 170 boil-off vapors can be removed from the liquid storage tank 170 as combined vapor stream 172 , 176 , reduced in pressure across one or more expansion devices 178 to form stream 180 , and vented to the atmosphere to control the pressure of the liquid storage tank 170 .
  • Heat exchanger 130 , expanders 134 , 158 and the associated piping may be insulated separately, for example, with an insulating material such as mineral wool, polyurethane foam, foamglass, “cryogel,” or a suitable alternative, or installed in small local cold boxes connected by insulated piping. Reducing the size requirements of the cold box is especially important when dealing with and scheduling shipping routes because certain destination locations may be hard or impossible to reach with larger pre-insulated loads (i.e., cold box loads).
  • the feed compressor 106 may also be eliminated, and in that case, the warmed tank flash and boil-off vapor stream 102 may be vented to the atmosphere through a valve to simply control the pressure of the liquid storage tank 170 .
  • stream 124 from the recycle compressor aftercooler 122 is split into two streams 226 and 228 that feed the compressor ends of the warm and cold companders 238 and 246 arranged in parallel.
  • the respective outlet streams 240 and 248 of the warm and cold companders 238 and 246 are combined into stream 249 and cooled in aftercooler 250 before being fed to heat exchanger 130 as stream 252 .
  • Stream 252 is cooled to a first intermediate temperature in heat exchanger 130 before being split into streams 232 and 253 .
  • Stream 232 is expanded in warm expander 234 to form stream 236 and combined with warming discharge stream 160 forming stream 162 at an intermediate location of the heat exchanger 130 .
  • Stream 253 is further cooled to a second intermediate temperature and split again into streams 256 , 254 .
  • Stream 256 is expanded in cold expander 258 to form discharge stream 160 .
  • Discharge stream 160 is then warmed in the heat exchanger 130 .
  • Stream 254 is further cooled in heat exchanger 130 to form the high pressure dense-phase stream 164 that is fed to the liquid storage tank 170 via expansion device 166 .
  • FIG. 3 is a flow diagram of a previously disclosed prior art process with the same expander configuration as shown in FIG. 1 but where the process comprises no flash vapor or boil-off recovery from the tank.
  • FIG. 3 is provided for exemplary purposes and to be used to compare with the system and process of FIG. 1 .
  • a cold end separator 304 and subcooler 310 are incorporated in the liquefier 301 and there is no recovery of the flash or boil-off vapor from the liquid storage tank 170 .
  • the high pressure dense-phase stream 164 from the cold end of the heat exchanger 130 is reduced in pressure in one or more expansion devices 300 and the resulting two-phase stream 302 is then fed to a separator 304 along with the cold expander discharge stream 160 that may contain some liquid.
  • Vapor stream 306 from separator 304 is warmed in heat exchanger 130 to an intermediate temperature where it is combined with the warm expander exhaust stream 136 to form stream 162 .
  • Liquid stream 308 from separator 304 is subcooled in subcooler 310 to about 78 K to form stream 312 .
  • a portion 316 of subcooled liquid stream 312 is reduced in pressure in one or more expansion devices 318 and then evaporated in subcooler 310 to form vapor stream 320 and reheated in heat exchanger 130 to form stream 102 .
  • the remaining portion 314 of subcooled liquid stream 312 is fed to the liquid storage tank 170 via one or more expansion devices 166 to form stream 168 where stream 168 is fed into the liquid storage tank 170 .
  • Flash and boil-off vapor from the liquid storage tank 170 is vented via stream 176 through expansion device 178 to form stream 180 (to be vented to the atmosphere) to control the tank pressure.
  • FIG. 4 is a flow diagram illustrating several exemplary options for integrating the liquefier system and process of FIG. 1 with an ASU or nitrogen generator.
  • the low pressure nitrogen feed stream 100 from the warm end of the ASU may be completely or partly replaced by one or more of alternative feed streams 400 , 404 , or 408 .
  • a high pressure nitrogen stream 400 from the warm end of the ASU or nitrogen generator may also be mixed with stream 112 from the feed compressor aftercooler 110 to form stream 402 that may then be mixed with stream 114 to form stream 116 that is fed to the recycle compressor 118 .
  • stream 400 may be mixed downstream of where stream 114 combined with stream 112 , or into an interstage location of the feed compressor 106 or recycle compressor 118 .
  • a low pressure nitrogen stream 404 from a low pressure column or subcooler at the cold end of the ASU may be mixed with the returning low pressure stream 174 from the liquid storage tank 170 to form stream 406 that is then heated in the heat exchanger 130 .
  • a cold high pressure nitrogen stream 408 from a high pressure column of the ASU or nitrogen generator or the single column of a single column nitrogen generator may be mixed with the discharge stream 160 from the cold expander 158 to form stream 410 that is then heated in heat exchanger 130 .
  • a divided portion stream 412 of the high pressure dense-phase stream 164 from the cold end of the liquefier may be fed directly to the ASU or nitrogen generator to provide refrigeration whilst the remaining portion 414 may be fed to the liquid storage tank 170 .
  • a “divided portion” of a stream shall mean a portion having the same chemical composition as the stream from which it was taken.
  • Divided portion stream 412 may be fed, for example, to the High Pressure (HP) column, the Low Pressure (LP) column, the subcooler, or the heat exchanger of an ASU.
  • Tables 1 and 2 provide exemplary flow rates, temperatures, and pressures for the configurations/processes of FIG. 1 and FIG. 3 .
  • the configuration/process disclosed in FIG. 1 resulted in the data of Table 1, where 300 tonnes per day of liquid nitrogen was produced in liquid storage tank 170 .
  • the configuration/process consumed approximately 5950 kW of electricity.
  • the exemplary process of FIG. 1 /Table 1 produces the same net quantity (446 kmol/hr) of liquid nitrogen in the liquid storage tank, but uses 0.8% less power than the previously disclosed process of FIG. 3 /Table 2, has a 3% lower feed rate (stream 100 ) due to the recovery of flash and boiloff vapor from the liquid storage tank (stream 174 ) and elimination of tank boil-off losses to atmosphere (stream 176 ), and provides significant capital cost savings from the elimination of a first separator, a second separator or subcooler, and their associated valves, controls and insulating enclosure.
  • the liquefier equipment may be insulated directly and the separate cold box structure required to contain and insulate the first separator, the second separator or subcooler, and their associated valves, and controls may be eliminated, thus, significantly reducing the size of the cold box. Reducing the size requirements of the cold box is especially important when dealing with and scheduling shipping routes because certain destination locations may be hard or even impossible to reach with larger pre-insulated loads (i.e., cold box loads).

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RU2013108796A (ru) 2014-09-10
TW201213692A (en) 2012-04-01
JP2013536392A (ja) 2013-09-19
WO2012013231A2 (fr) 2012-02-02
SG186906A1 (en) 2013-02-28
CN103270381B (zh) 2016-04-13
EP2598815A2 (fr) 2013-06-05
WO2012013231A3 (fr) 2013-04-25
KR20130056294A (ko) 2013-05-29
CN103270381A (zh) 2013-08-28
RU2531099C1 (ru) 2014-10-20

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