Apparatus and process for liquefying gases

Description

FIELD OF THE INVENTION

The present invention relates to liquefying gases, and more particularly to an apparatus and process for liquefying gases such as nitrogen and oxygen using an air separation plant for the source of the nitrogen and oxygen, and having a top running pressure of about 420 psig without requiring electrical compressors to build this pressure. This is made to reduce the power bill.

BACKGROUND OF THE INVENTION

Systems and methods for liquefying gases such as nitrogen and oxygen are well-known. The main process of producing large amounts of liquid nitrogen, oxygen, and argon is with an air separation plant. An air separation plant takes in atmospheric air and through a process of fractional distillation at cryogenic temperatures the component gases, or fractions, can be separated by their boiling points. There are other processes to separate air into its different gases, such as pressure swing absorption, vacuum pressure swing absorption, and others, but these are not making a transportable liquid. Today the production of a transportable liquid gas in large quantities requires a large number of compressors and expanders with all of the associated equipment such as cooling towers that require large amounts of electrical power to run at a high cost.

The process of making liquid gas today is to take gaseous pure nitrogen from two exiting streams of the main heat exchanger's warm side, one stream being the larger flow which is the low pressure nitrogen stream, and the other nitrogen stream having about half the flow but being higher in pressure. The larger flow, lower pressure 2 psig+/−1.5 psig nitrogen gas, along with the flash pot return flow from the liquefier section, this multi low pressure flow comes from the exit of two heat exchanger's warm sides. This low pressure flow is not all used and some is vented back to the atmosphere, while the remaining flow is sent to a low pressure nitrogen compressor, where the exit of the compressor is equal in pressure to the higher pressure multi feeds. The higher pressure flow is made of the exit of the main heat exchanger along with the exit of the low pressure nitrogen compressor and the gas off of the liquefier heat exchanger turbine return's warm side. All of the gas is sent to the recycle compressor, and then all of the gas is split to two turbine boosters. After each stage of compression the heat of compression is removed. This flow will be cooled down in four steps. The first step is the split off of gas to the warm turbine expander, and the second step is the split off of gas to the cold turbine. The remaining flow exits the liquefier heat exchanger where the gas is called a Soto liquid. The third step is to reduce the flow in pressure through a needle valve causing a Joule Thompson effect. The exit of the needle valve provides a two-phase liquid. The fourth step is to cool the liquid and gas down to all liquid, which is done in the flash pot. That is all the refrigeration needed.

Existing air separation plants designed to make liquids for sale in the industrial gas market normally use a liquefier. Current liquefiers make only a small amount of liquid per recycle pass (about 15.2% of the recycle compressor flow). Once the liquid is made, it is flash potted to become subcooled, and a small amount of liquid is returned to the air separation plant for refrigeration, while, the larger part of this liquid is sent to a storage tank. No liquid nitrogen is returned to the liquefier. There remains a need for an improved liquefier device.

BRIEF SUMMARY OF THE INVENTION

The present invention is directed to a system, apparatus and process for liquefying gases such as nitrogen and oxygen. The presented system is an open loop refrigeration system which uses far less electrical power than existing liquefaction systems, and can be gradually implemented to replace existing systems, as existing power contracts which typically have a term such as five years expire.

In an embodiment, the liquefier device is one part of an air separation plant, and in another embodiment is a retrofit to an existing plant. The same process can take almost any gas to a liquid. For purposes of illustration, there is shown diagrammatically in FIG. 1 an air separation plant having an air flow coming in of 780,000 scfh at the inlet meter point 111. The nitrogen, points 203 and 216 in FIG. 1, and oxygen, point 321 in FIG. 1, utilized by the liquefier device of the invention is produced by high pressure column 114 and low pressure column 116 (there are some plants that have three main columns) of the air separation plant. These nitrogen and oxygen flows will exit from a stable running air separation plant's main heat exchanger 113 warm side as pure oxygen gas at 321, and the two streams of nitrogen gas at 203 and 216 in FIG. 1 to be liquefied. In the illustrated embodiment, the liquefier device will be part of a retrofit to an existing air separation plant. All air separation plants can use this liquefier. In FIG. 1, the oxygen at point 321 exits the main heat exchanger 113 warm side with a temperature of 37 degrees Fahrenheit at a pressure of 19.928 psia and a flow of 161,521.037842 scfh. The nitrogen stream exits the main heat exchanger 113 to point 216 at 14.94 psia with a flow of 371,184.701923 scfh holding 37.29 degrees Fahrenheit, and the nitrogen stream exits heat exchanger 113 to point 203 at a pressure of 67 psig with a flow of 211,000 scfh holding 37 degrees Fahrenheit.

The oxygen stream 321 and the nitrogen streams 203 and 216 are fed to the liquefier device, which is an open loop refrigeration unit that takes in the separate streams as a pure gas and which streams will exit the liquefier device as a saleable liquid nitrogen at point 537 (see FIG. 6) and liquid oxygen at point 381 (see FIG. 8). The liquefier device of the present invention has significantly reduced power requirements as compared to conventional liquefiers and therefore can produce saleable liquids less expensively.

The present system takes advantage of many properties of liquid nitrogen. One of these properties is that liquid nitrogen is mostly a non-compressible fluid that can be pumped up in pressure which occurs in the liquefier device at point 528 (FIG. 6), which will take less force than compressing a compressible gas to achieve runnable pressures. The liquid nitrogen streams can be brought up in pressure by a pump (either liquid nitrogen pump 169 or 170 in FIG. 6), which pump in the embodiment shown is using less than 100 horsepower. Then, the liquid is brought to a heat exchanger (boiler 145 in FIG. 4) where the pumped liquid at point 528 in FIG. 4 is boiled to a vapor point. The pressure vapor point of the vapor is held back by the four variable guide vanes in turbines 154, 158, 162, and 166, all of which are shown in FIG. 5. The vapor produced can then be used to run the four turbine expanders 153, 157, 161, and 165, also shown FIG. 5. The exit of the turbine expanders at point 450 in FIG. 5 yields a lower pressure gas, with a temperature almost at its boiling point, which is directed into a phase separator 151 and then to add refrigeration to the condenser 146 in FIG. 4, which makes more liquid. The turbine expanders' exiting gas will remove the latent heat of vaporization from the higher pressure nitrogen stream at point 500 to the point 149, and the lower pressure oxygen stream at point 332 to the point 305 all in FIG. 4.

Some conventional air separation plants might have an oxygen and/or nitrogen pipe line which will take the gas described here to another compressor for the pipe line's use. The remaining gas can be used along with any gas the pipe line compressor would vent from time to time. Although not illustrated, it will be understood that these types of changes are able to be performed with a minimum number of modifications or changes to the air separation plant and the liquefier device of the present invention.

Additional areas of applicability for the present invention will become apparent from the detailed description provide hereinafter. It should be understood that the detailed description and specific examples of this preferred embodiment of the invention are intended for purposes of illustration only, that the temperatures, pressures, and purities shown here are close to actual readings but may not be exact, and are not intended to limit the scope of the invention. Other embodiments could be, for example, for the production of liquefied natural gas.

BRIEF DESCRIPTION OF THE DRAWINGS

The present invention will become more fully understood from the detailed description and the accompanying drawings, wherein:

FIG. 1 is a schematic diagram of a main plant air separation unit configured for operation with the liquefier device of the present invention.

FIG. 2 is a schematic diagram of the general operation of the argon liquefaction system in accordance with the present invention.

FIGS. 3a-3c are schematic diagrams of the oxygen and low and high pressure inlet piping for the liquefier device of the present invention.

FIG. 4 is a schematic diagram of the heat exchangers of the liquefier device of the present invention.

FIG. 5 is a schematic diagram of the turbine and booster system of the liquefier device of the present invention.

FIG. 6 is a schematic diagram of the liquid nitrogen pump system of the liquefier device of the present invention.

FIG. 7 is a schematic diagram of the backup gas nitrogen system of the liquefier device of the present invention.

FIG. 8 is a schematic diagram of the air separation plant liquid oxygen filter house.

DETAILED DESCRIPTION OF THE INVENTION

The following detailed description is of the best mode or modes of the invention presently contemplated. Such description is not intended to be understood in a limiting sense, but to be a non-limiting example of the invention presented solely for illustration thereof, and by reference to which in connection with the following description and the accompanying drawings one skilled in the art may be advised of the advantages and construction of the invention.

The following detailed description will describe the liquefier device of the present invention with reference to an air separation plant site having an inlet gas air flow of 780,000 standard cubic foot per hour at the inlet meter box, and will make over 650 tons a day of saleable liquids, running with the liquefier device.

THE BASE LINE. The inventor will first explain one way an air separation plant making over 650 ton a day of liquid product could run. The following explanation is based on an oxygen content of 4 ppm and zero argon on all pure nitrogen streams, and on a standard cubic foot of gas at one atmosphere and at 70 degrees Fahrenheit. The plant site location is around sea level, with an 80 degree Fahrenheit dry bulb temperature and a 70 degree Fahrenheit wet bulb temperature. In addition, the Table included herein provides temperature, pressure, and flow readings for each reference numeral point or step within the air separation plant and liquefier device assembly as described herein with reference to the FIGS., as well as the Figure location, and other comments.

THE AIR SEPARATION PROCESS. Referring now in particular to FIG. 1, the air around us is the air 1 used by the air separation plant to make saleable liquids, and initially is to be filtered at filtering system 100. Normally there is a four-stage compressor 101 used to bring up the air to a runnable pressure, and three intercoolers that will remove condensed water at 102. After the fourth compression stage there is a possible vent valve 103 which is normally closed. The compressed air is now cooled with a fan cooled aftercooler 104, then cooled again with refrigeration unit 105. Water is condensed during compression and is sent to the water separation unit 106 where the water is removed at 107. The air is still holding a lot of moisture and must be dried down to −110 degrees Fahrenheit due point, which is achieved by a molecular sieve bed 108. The drying action will break up a small amount of the sieve material into a fine dust that is now removed by the dust filter 110. The air is now ready to use.

There is a line to the instrument air supply header controlled by an on/off valve 112 normally open to send a supply of filtered air to the backup gas nitrogen system (see FIG. 7) at point 2. All the rest of the air is metered at 111 and sent through line 3 entering the insulated cold box 49 to the main heat exchanger 113. The air exiting the main heat exchanger 113 in line 4 is sent to the third tray of the high pressure column 114. Condensed liquid will fall to the bottom of the high pressure column 114 and will be removed in line 5. This liquid at point 6 must be cooled by a subcooler 117 prior to being elevated in line 7 to point (8) and split into either line 9 to the top of crude argon condenser 120 or into line 10 to the 44th tray of the low pressure column 116. Referring again to the high pressure column 114, the rest of the gas that entered into the column 114 moves up the column thru 38 trays, and is removed at the top of the column 114 in line 200 as pure nitrogen gas. The nitrogen gas in line 200 splits off to line 201 which leads into the tube side of the reboiler 115 inside the low pressure column 116 bottom liquid. The reboiler 115 will condense the gas nitrogen to a liquid nitrogen. This liquid nitrogen flow exiting the reboiler in line 220 will also be split, with most of the liquid nitrogen to be returned to the high pressure column 221, and the rest will be directed in line 222 to the subcooler 117.

In addition to splitting off to line 201, there is a stream of pure nitrogen gas off the high pressure column 114 in line 200 that will be removed in line 202 to the main heat exchanger 113, where the gas nitrogen stream is warmed and exits the main heat exchanger 113 at point 203. The gas is then directed to the high pressure nitrogen inlet line to the liquefier, shown in FIG. 3c. Referring again to FIG. 1, most of the liquid nitrogen flow in line 220 exiting the reboiler 115 is directed in line 221 to the high pressure column 114, but the remainder is directed in line 222 to the subcooler 117. The subcooler 117 will remove more heat from the liquid flow so that upon exiting the subcooler 117 in line 223, the flow can be used in the low pressure column 116 without a major flash off. The liquid is elevated to the top of the low pressure column 116 to a control valve in line 224 that will meter, and depressurize the flow. The amount of liquid nitrogen needed to make up the heat loss of the main operation is added at point 549 from point 544 (FIG. 6), which is the flow from the new liquefier. Prior to reaching point 549, the flow of liquid nitrogen from point 544 is split, such that one flow is directed to the pure argon system (FIG. 2 point 545) and another flow is directed to a control valve 548 that will meter and depressurize the flow at point 549, which as indicated above is joined by the flow in line 224 resulting in a joined flow in line 225.

The joined flow 225 will enter the low pressure column 116 at tray 65. The gas at the top of the low pressure column 116 exiting in line 210 is mostly nitrogen. The liquid nitrogen from the liquefier device in line 544 that is directed to the pure argon system (FIG. 2, point 545) will return as a low pressure nitrogen gas (FIG. 2 point 558) and is joined with the low pressure 210 nitrogen gas exiting the low pressure columns 116 in line 210, and the joined flow in line 214 is directed to the subcooler 117. The exit of the gas nitrogen from the subcooler 117 in line 215 will now enter the main heat exchanger 113, and the low pressure nitrogen gas then exits the main heat exchanger 113 to the low pressure nitrogen inlet line to the liquefier device of the present invention, shown at point 216 in FIG. 3b.

Referring again to the low pressure column 116 in FIG. 1, going down the column to tray 55, this is the point where waste nitrogen and a large amount of carbon monoxide will exit the process. The waste nitrogen stream 50 exits the low pressure column 116 to the subcooler 117. At the exit of the subcooler (117) in line 51 the waste nitrogen stream enters the main heat exchanger 113, and then exits the main heat exchanger 113 in line 52 a warmed stream to a control valve where the flow is metered. After the control valve the warmed waste nitrogen stream in line 53 is then used to reactivate the molecular sieve bed 109, which is off line. The waste nitrogen stream 53 is therefore sent to the tube side of a gas fired heater 122 and then will exit in line 54 to the top of the off line molecular sieve bed 109. The bed is first heated, then cooled by the waste nitrogen, and the gas will exit to atmosphere at line 55. Referring still again to the low pressure column 116, going down the column to tray 44, this is the location where the liquid in line 10 from the bottom of the high pressure column 114 will enter. The liquid in line 9 from the bottom of the high pressure column 114 enters the crude argon condenser 120, where it is used to condense the crude argon in the tube side of the reboiler 119. A small amount of the liquid from the bottom of the high pressure column feed in line 9 will be removed in line 11, where it is metered and then sent in line 12 to the low pressure column 116 tray 42. The rest of the liquid from line 9 exiting the bottom of the high pressure column 114 is vaporized during the condensing of the crude argon in the reboiler 119. The gas formed from such vaporization exits the high pressure column 114 in line 13 and is metered by a control valve, and afterwards is brought line 14 to the 43rd tray of the low pressure column 116. Going down the low pressure column 116 to tray 24, this is the location where the amount of argon gas is the highest in the low pressure column. This gas is fed line 15 to the crude argon column 118. The liquid at the bottom of the crude argon column 118 exits in line 16 to a metered control valve. After the control valve the liquid in line 17 is sent back to the 24th tray of the low pressure column.

Staying with the crude argon column 118, the gas in line 15 from the low pressure column 116 enters the crude argon column and rises to the reboiler 119 thru 38 trays. The gas will turn to liquid and gas in the reboiler 119 tube side. The liquid and gas will exit to the phase separator 121, and the gas off of the phase separator 121 is directed to the argon liquefaction system (FIG. 2, point 400). The liquid from the phase separator 121 is directed to the crude argon column 118, tray 38. Back to the low pressure column 116, going down the column to just below the tray number one, the gas found here is called “pure oxygen.” The gas oxygen will be removed from the low pressure column 116 in line 320 to the main heat exchanger 113 where the gas is warmed. After the heat exchanger, the warmed gas is directed to the oxygen inlet line to the liquefier device (see FIG. 3a, point 321). Back to the low pressure column 116, the bottom liquid is “pure liquid oxygen.” The reboiler 115 is changing the liquid oxygen into gaseous oxygen that drives the low pressure column 16. Most of the gas will go up the column, but the process of removing a large amount of gas oxygen will cause a lower pressure. The lower pressure will mean a lower temperature, which will lower all running pressures all the way back to the main air compressor 101. The small amount of liquid oxygen will need to be removed in line 300 to flush out the solid contamination. This liquid oxygen will be sent to the subcooler 117, and after the subcooler 117 the flow in line 301 will be metered but the level control of the reboiler height will be valves 336, or 343, or 357 in FIG. 8. The liquid oxygen flow is sent to FIG. 8 at point 302. Also referred at the bottom of FIG. 1 is point 40 from FIG. 7, which is a cold box nitrogen purge used to keep a positive pressure on the insulated cold box 56 to keep out the wet air. Another set of points come around the low pressure column 166 feed 211 to the safety relief valve 213 and burst disk 212, which set up is cold and needs a warming nitrogen flow which it receives from FIG. 7 point 39 to insure it works when needed.

THE PURE ARGON SUBSYSTEM. Referring now primarily to FIG. 2, there are two major flows shown, one of which is the nitrogen for cooling, and the other is the argon to process. The nitrogen flow comes in from FIG. 1, point 545 as a cool liquid nitrogen that will branch off to two control valves, both of which control valves control the liquid nitrogen baths they are supplying. The flow out of line 546 is to the pure argon recondenser holding tank 126 that will bottom fill the heat exchanger 125 shell side. The liquid nitrogen will be vaporized and exit in line 555 to a pressure control valve and then to line 557. The second flow from FIG. 1, point 545 goes to another control valve set to hold a liquid level in line 547 on the shell side of the pure argon column condenser 131. This liquid nitrogen will be vaporized and exit the condenser 131 in line 556 to a pressure control valve, after which it will join line 557 and head back to the main air separation unit at FIG. 1, point 558.

The argon to process comes in from FIG. 1, point 400. This crude argon flow will enter the cold side of argon heat exchanger 133 and exit warm in line 401 heading to a joined flow with line 403 of hydrogen. The joined flow 404 is directed to the argon compressor 134, which is a two stage compressor with one intercooler. The compressed argon hydrogen flow exiting the argon compressor 134 in line 405 is cooled by an after cooler 135 and exits the aftercooler 135 in line 406 to be joined by a make-up flow of hydrogen. The make-up flow of hydrogen comes from a tube trailer 136, exits to a small line 407 then is pressure regulated to supply 408 to the compressed argon hydrogen flow 406 to make the combined flow 409 to the argon flash arrester 137. Upon exiting the flash arrester 137 at line 410, the flow is directed to a deoxo-catalyst bed 138 where the hydrogen and oxygen in the argon will be combined to make water vapor. The name of the flow at this point changes to combusted argon. The exit of the deoxo-catalyst bed 138 in line 411 is very hot with a lot of humidity. The combusted argon flow is now cooled by an aftercooler 139, after which the high humidity will now be water in line 412. Next, the water is removed using a phase separator 140 with a bottom water drain control valve exiting to atmosphere at 432. The combusted argon is still at 100% relative humidity upon exiting the phase separator 140 in line 413. The combusted argon must be dried to −110 degrees Fahrenheit dew point, and so the flow is sent to a drier bed 141. At the exit of the drier bed 141 in line 414 there is some dust with the combusted argon, which is removed by a dust filter 143. Now the combusted argon in line 402 is dry, dust free and ready to be used, and is directed to an argon heat exchanger 133.

The combusted argon 402 is warm as it enters the argon heat exchanger 133. At the cold side of the argon heat exchanger 133 the flow 415 is directed to a hydrogen separator 127, and is almost forming a liquid as it enters the hydrogen separator 127. The gas in line 416 upon exiting the hydrogen separator 127 will rise to the tube side of the argon reboiler 128 due to the condensing action of the reboiler. The reboiler 128 is not cold enough to liquefy the left over hydrogen from the deoxo-catalyst bed 138, and therefore will collect at the top of the reboiler tube side and all the argon and nitrogen will liquefy and fall at 417 to the bottom of the hydrogen separator 127, as there are no trays here. The hydrogen at the top of the reboiler is removed at 419 to a flow control valve and is sent back in line 403 to joined suction flow 404 of the argon compressor.

The liquid at the bottom of the hydrogen separator 127 is removed at 418 to a level control valve that in line 420 feeds the pure argon column 130. This flow contains argon and nitrogen, with a trace of oxygen and hydrogen. This liquid was not subcooled and will flash after decompression. The liquid and gas mixture will separate, and the gas will rise thru distillation trays and the liquid will overflow the tray to the tray below until it collects at the bottom.

The liquid at the bottom of the pure argon column will first collect around the outer shell ring 129 of the reboiler shell side 128, and after that ring is full, the liquid will fill the bottom of the pure argon column 130. This liquid is then removed at 425 to a level control valve and is joined at 427 with the recondensed argon in line 431 heading to the pure argon tank 124. The gas that entered the pure argon column 130 will rise thru distillation trays until it is condensed in the tube side of the condenser 131. The condenser 131 shell side is full of liquid nitrogen and this makes it cold enough to liquefy in line 421 the nitrogen in the argon but will not liquefy the hydrogen. The liquid and gas bubbles will be removed in line 422 to the phase separator 132. A small amount of gas is removed to a flow control valve that exits at 423 to atmosphere. This valve is always very cold and needs a warming purge flow, which is received from the backup gas nitrogen system (FIG. 7, point 37). The liquid of the phase separator 132 exits in line 424 back to the pure argon column 130 top tray and acts as a cold cap stopping gas argon from passing.

The argon in the storage tank 124 has a vent line 428, and the argon transport trailer 123 has a similar vent line 429 both of which will vent excess pressure through a vent auto pressure control valve. The vented gas will share the same line at 430 to the tube side of the argon recondenser 125 where it will be liquefied, and in line 431 the liquid is returned to the joined line 427 to the argon storage tank 124.

There are two argon dryer beds used in this process, identified in FIG. 2 at 141 and 142. As illustrated in FIG. 2, dryer bed 141 is shown as the dryer being used, and dryer 142 is on reactivation. The reactivation is performed by the nitrogen off of the purge header from FIG. 7, point 36. The dryer vessels have their own heaters and only need a dry gas nitrogen to move the contamination out to vent at 433.

THE TAKE OR VENT INLET PIPING TO THE LIQUIFER. As illustrated in FIGS. 3a-3c, there are three inlet flows to the liquefier, all three of which come from the air separation plant main heat exchanger's warm side (FIG. 1). These are the gas oxygen inlet flow, the gas nitrogen inlet flow from the low pressure side of the air separation plant main heat exchanger's warm side, and the gas nitrogen inlet flow from the high pressure column.

Referring now to FIG. 3a, the gas oxygen inlet flow as shown comes from the warm side of the main heat exchanger, FIG. 1, point 321. This gas oxygen flow is now controlled by a flow meter 325 in order to prevent or stop an over draw of production. The flow is set by the air separation plant, and if the reading of flow meter 331 is not equal to flow meter 325 then any excess flow will be vented. The venting of excess gas oxygen is seen by flow meter 327, which controls the vent valve 329. If the pressure is too high the relief valve 328 will open. If the flow meter 327 shows a flow, then there is a problem. Valve 326 is the main flow control. There is a check valve 330 feeding the flow meter 331. The exit of the inlet process is oxygen gas to the liquefier at FIG. 4, point 332.

In FIG. 3b, the low-pressure gas nitrogen flow is shown coming from the warm side of the main heat exchanger in FIG. 1, point 216. This low-pressure nitrogen flow is now controlled by flow meter 250 to stop an over draw of production. The flow is set by the air separation plant, and if flow meter 256 is not equal to flow meter 250 then any excess will be vented. The venting of excess is seen by flow meter 252 which controls the vent valve 254. If the pressure is too high the relief valve 253 will open. If the flow meter 252 shows a flow then there is a problem. Valve 251 is the main flow control. There is a check valve 255 feeding the flow meter 256. The exit of the inlet process is to the liquefier at FIG. 4, point 257.

In FIG. 3c, the gas nitrogen flow from the high-pressure column comes from the warm side of the main heat exchanger in FIG. 1, point 203. This high pressure nitrogen flow is now controlled by flow meter 231 to stop an over draw of production. The flow is set by the air separation plant, and if flow meter 237 is not equal to flow meter 231 then any excess will be vented. The venting of excess is seen by flow meter 233 which controls the vent valve 235. If the pressure is too high, the relief valve 234 will open. If the flow meter 233 shows a flow, then there is a problem. Valve 232 is the main flow control. There is a check valve 236 feeding the flow meter 237. There is also a two-inch branch line feeding an on or off valve 238 that feeds a purge nitrogen gas supply to FIG. 7, point 33. The main exit of the inlet process is to the liquefier in FIG. 4, point 239.

THE LIQUIFIER. Referring now to FIG. 4, the heat exchangers and flash pots for the liquefier device are illustrated diagrammatically. This is located in a well-insulated box 48 with a nitrogen purge coming in from the backup gas nitrogen in FIG. 7, point 41. The three gas streams described with reference to FIGS. 3a-3c from the air separation unit will enter the liquefier at different points. The oxygen gas stream comes in to the liquefier device cold box 48 from FIG. 3a, point 332. The oxygen gas stream flow is passed sequentially through three heat exchangers, namely, oxygen cooler 144, boiler 145, and condenser 146, and then enters the tube side of oxygen flash pot 147. The exit of the flash pot tube side will be a subcooled liquid oxygen, which is directed to the liquid oxygen filter house shown in FIG. 8, point 305. The draw of oxygen will be the change of state from gas to liquid. There is a change of pressure needed to make the pressure of the liquid oxygen here higher than the low-pressure column's feed. This change in pressure is accomplished by the height of the flash pot 147. The flash pot 147 should be about fifteen feet higher than the low pressure liquid oxygen line off of the low pressure column heading to the oxygen filter house. This means the gas oxygen stream to the flash pot should not be cold enough to condense prior to the entrance to the flash pot 147.

The low pressure nitrogen gas stream to the liquefier device comes in from FIG. 3b, point 257. This low pressure nitrogen stream joins the flow downstream from pressure exit control valve 264, and the combined flow in line 265 exits to the turbine boosters in FIG. 5, at point 265.

The high pressure column gas nitrogen stream to the liquefier device comes in from FIG. 3c, point 239. This stream joins the equal pressure flow downstream from the line exit of control valve 455, forming the combined flow 462. This combined nitrogen stream flow 462 will now branch off to two lines containing control valves 456 and 457. Control valve 456 will add heat to the heat exchanger 152 called the preheater. The exit of the preheater 152 and the exit of the auto control valve 457 will join and exit to turbine package in FIG. 5, at point 458.

In addition, there is a flow from the turbine package or assembly, FIG. 5, point 273, to an auto control valve 274 (FIG. 4) that will add heat to the preheater 152 and exit back to the turbine at FIG. 5, point 275. There is also a flow off of the boiler 145 going to the preheater 152 that needs to be warmed prior to being decompressed as shown FIG. 5, point 288.

The major flow of compressed nitrogen gas from the turbine assembly at FIG. 5, point 500 branches off to three auto control valves 501, 502, and 503. Auto control valve 501 will be set to warm the oxygen cooler 144. The exit of the flow 501 will join the exit flows of 502 and 503. The exit of auto control valve 503 will warm the preheater 152. The auto control valve 502 will bypass the heat exchangers and move a warm gas flow into the boiler 145. The boiler 145 has a liquid nitrogen bath that must be boiled away. The gas nitrogen from the three auto control valves (501, 502, and 503) will boil the liquid nitrogen in the boiler 145. The gas from line 500, FIG. 5 will be cooled off but will not condense, but the liquid nitrogen bath in the boiler 145 will turn to gas nitrogen. The cooled-off gas nitrogen from point 500 will go to the next heat exchanger 146 called the condenser, where the gas nitrogen is exchanging its heat with the exhaust of the four turbines, making the gas into a two-phase liquid gas nitrogen stream.

The two-phase stream is sent to the next heat exchanger 150 called the added cooling heat exchanger. Here the two-phase nitrogen stream will be cooled a little more but will still be a two phase stream at the exit. The two-phase stream is then directed into the pump flash pot 149 tube side where the nitrogen stream will be all liquid. The exit temperature at the pump flash pot 149 will be set to hold a boiling point of the boiler 145 after the pump. The liquid nitrogen is cold enough to be used. The liquid nitrogen off of the pump flash pot 149 will branch off to five places, which are to the liquid nitrogen pump (FIG. 6 point 510), then to the air separation plant (FIG. 6 point 511), then to the auto control valve 512 back feeding the pump flash pot 149, then to the tube side of the nitrogen production flash pot 148, and lastly to the auto control valve 513 feeding the shell side of the oxygen production flash pot 147.

Transition from FIG. 4 to FIG. 6. Following the flow of liquid nitrogen off of the pump flash pot 149 to the liquid nitrogen pump (FIG. 6 point 510), this liquid nitrogen flow can bypass the pump during start up, through a branch line containing valve 522. After the pump is running, there is a check valve 523 which will stop a back flow until the valve 522 is closed. A flow from the auto control valve 522 thru check valve 523 can supply the boiler through line 528 (to FIG. 4) and the pump flash pot through line 529 to valve 530 in FIG. 4. [As an operation note, starting a pump sometimes needs priming, and the priming can be done to a low pressure point using the pump flash pot shell side thru FIG. 4, point 529 opening valve 530 as valve 522 (in FIG. 6) is closing.]

Two separate liquid nitrogen pumps 169 and 170 are shown in FIG. 6, which are used for the movement of the liquid nitrogen to the boiler. Two pumps 169 and 170 are provided because the carbon seal on the pumps will wear out, and providing two pumps will allow the operation to stay running as the pumps are switched to replace the carbon seal. Only one pump should be running at a time. In FIG. 6, the inlet valve to the pump 169 is auto valve 520, and the exit valve is auto valve 524, which will feed a check valve 526. The inlet valve to the pump 170 is auto valve 521, and the exit valve is auto valve 525, which will feed a check valve 527. Flow from the pump in use will branch off to the heat exchangers in FIG. 4, point 529 to check valve 530 feeding flash pot 149, and FIG. 4, point 528, where it will feed the boiler 145. The amount of liquid to the boiler 145 will be regulated by the bypass level control valve 523 if the pump is off, or a slowly changing pump speed. The flow from FIG. 6, line 529 to FIG. 4 goes to auto control valve 530. The flow thru level control valve 530 is to the shell side liquid level of the pump flash pot 149 and this is normally closed.

The next branch off of the pump flash pot 149 in FIG. 4 is to FIG. 6, point 511. There is a dump to atmosphere branching from line 511 through auto control valve 542. Line 511 also leads to a normal running open valve 543 this will close check valve 541 and go to line 544 as the liquid back to the air separation plant (see FIG. 1). If the liquefier is not able to feed the air separation plant, then liquid from the nitrogen storage tank 171 is used. A liquid flow off the nitrogen storage tank 171 is provided by opening valves 539 and 540. After starting the liquid pump 172 the nitrogen flow will go to check valve 541, then to a closed auto valve 543, then to line 544 feeding the air separation plant. At all times, the flow to the air separation plant is controlled by the level controls of the pure argon condenser 131 flow through line 547, the level controller of pure argon recondenser 126 flow through line 546, and the metered flow at line 549 to the low pressure column.

The next branch off from the pump flash pot 149 is to the level controller valve 512 (FIG. 4) sending liquid back to the shell side of the pump flash pot. This is normally closed. The next branch off from the pump flash pot 149 is to the level controller valve 513 (FIG. 4) sending liquid to the shell side of the oxygen production flash pot (147). This is also normally closed.

The last branch off from the pump flash pot 149 is to the tube side of the nitrogen production flash pot 148 (FIG. 4). The liquid nitrogen exiting the flash pot 148 branches to valve 514 and to line 515 (see FIG. 6). The valve 514 is a liquid level control valve to control the liquid height of the shell side of the nitrogen production flash pot 148. This is normally closed. The branch off to line 515 is the production liquid nitrogen to the nitrogen storage system. If the production is not good it will be sent to dump thru valve 535. When the liquid nitrogen is found to be good there is a last purge valve 536 prior to the tank valve which is normally closed. The valve 537 is the production metering valve and is the entry to the nitrogen storage tank 171. The nitrogen storage tank 171 will be monitored to one psig. The tank venting will be thru valve 538 to atmosphere. The liquid temperature to control the venting will happen in the production flash pot 148 liquid level and the gas exit pressure 459 (see FIG. 4).

Referring now to the liquid nitrogen feed to the boiler 145 in FIG. 4 from line 528, FIG. 6, after the liquid nitrogen leaves the pump flash pot 149, the liquid must be cool enough to stay as single phase liquid thru the pumping stage then up to the boiler, but not be too cool to stop the boiling action when it enters.

Vaporized nitrogen coming out of the boiler 145 is routed to the preheater 152. The preheater 152 can be warmed by three flows, namely: the booster four aftercooler exit called the major flow controlled by valve 503, the booster one aftercooler exit controlled by valve 274, and the high pressure column and turbine exhaust flow controlled by valve 456. This can be monitored by the auto opening of valve 451. Valve 451 will drain excess liquid produced by the four turbines that is not used by the three flash pots.

The exit of the vaporized nitrogen flow from the preheater 152 goes to the turbine assembly illustrated in FIG. 5, at point 288. This nitrogen gas is sent to four flow meters 289, 290, 291, and 292. Each flow meter is connected to its own turbine expander and sets the variable guide vanes for each turbine expander. Flow meter 289 is the inlet to turbine expander 153. Flow meter 290 is the inlet to turbine expander 157. Flow meter 291 is the inlet to turbine expander 161. Flow meter 292 is the inlet to turbine expander 165. The guide vanes 154 of turbine expander 153 are set by flow meter 289, the guide vanes 158 of turbine expander 157 are set by flow meter 290, the guide vanes 162 of turbine expander 161 are set by flow meter 291, and the guide vanes 166 of turbine expander 165 are set by flow meter 292. All four turbine expanders exit to a common header with one exit (to FIG. 4, point 450).

Point 450 in FIG. 4 is where the exit from the four turbine expanders goes into a phase separator 151. The phase separator 151 will hold a liquid level controlled by the exit temperature of the turbines and the draining four auto control valves. The temperature of the turbine exit has to do with the pressure of the boiler 145 and the feed temperature from the preheater 152. The four auto control valves are the over flow valve 451, the filling of the shell side of the oxygen production flash pot 147, valve 452, the filling of the shell side of the nitrogen production flash pot 148, valve 453, and the filling of the pump flash pot 149, valve 454.

Filling of the oxygen production flash pot 147 shell side by a level control valve 452, this should be the only filling valve needed for the flash pot 147. Another valve 513 is provided in cased it is needed but is closed on normal operation. The liquid nitrogen being supplied to the flash pot 147 by level control valve 452 is not subcooled and will flash when decompressed. The rest of the liquid will boil away as the tube side liquid oxygen is cooled. The exit oxygen temperature control is from the liquid height of the nitrogen shell side bath, and the pressure held on the exit nitrogen gas in line 461. The vent valve 382 on the oxygen storage tank 177 (see FIG. 8) is the only a pressure control valve on the tank, but the valve should not be always open. The opening of the vent valve 382 should be monitored and the temperature of the oxygen production flash pot 147 should be controlled. The oxygen storage tank should never run below 0.5 psig or above 1.5 psig without an adjustment, and the vent valve 382 will open at one psig.

Looking at the nitrogen production flash pot 148 in FIG. 4, auto level control valve 453 is the only valve that should be used to fill the shell side of the nitrogen production flash pot 148. Valve 514 is also there if needed, but is closed during normal operation. This liquid nitrogen passing through control valve 453 will come in without subcooling and will flash when decompressed. The rest of the liquid to the shell side from valve 453 will be boiled off, as the liquid nitrogen on the tube side is cooled. There is a vent valve 538 on the nitrogen storage tank 171 (see FIG. 6). The exit production liquid nitrogen temperature control is from the liquid height of the nitrogen shell side bath, and the pressure held on the exit nitrogen gas in line 459. The vent valve 538 on the nitrogen storage tank 171 is the only pressure control valve, but the valve should not be always open. The opening of the vent valve 538 should be monitored and the temperature of the nitrogen production flash pot 148 should be controlled. The nitrogen storage tank 171 should never run below 0.5 psig or above 1.5 psig without an adjustment, and the vent valve 538 will open at one psig.

The pump flash pot 149 has a level control valve 454 which should be the only liquid nitrogen supply to the shell side. Other valves, including valves 530 and 512, should be closed and are there if needed. The pump flash pot 149 tube side liquid nitrogen must be monitored to control its flash off point. The liquid should be a single phase as it exits the nitrogen pump, but not so cold that it stops the boiler as it enters. The tube side liquid nitrogen therefore has to be monitored and the shell side liquid nitrogen height and pressure controlled.

After all three flash pots 147, 148, and 149 have taken what they need from the three percent of produced liquid off of the turbine exhaust phase separator 151, there should be a small amount left over. This is passed through a level control valve 451 and liquid that is not subcooled will flash when decompressed. The flashing liquid nitrogen is put into a low pressure line used by the nitrogen production flash pot exhaust gas. As this valve 451 opens and closes it will show how the exit temperature of the four turbines are doing. If the valve 451 closes a little, that shows more liquid is being used by the flash pots, or the preheater is running to warm, or the boiler pressure is changing to a lower pressure.

The three flash pots 147, 148, and 149 shell sides will exit gas nitrogen. The oxygen production flash pot 147 will exit the shell side nitrogen gas in line 461 to the condenser 146. At the exit of the condenser pass there is a branch off to a pressure control valve 260 or a check valve 261. Check valve 261 will take a small flow during startup to the turbine exhaust header but when the turbine exhaust pressure goes above the flash pot pressure auto pressure control valve 260 will move the gas to a low-pressure line. During normal operation, check valve 261 is closed and pressure control valve 260 is controlling. The nitrogen production flash pot 148 shell side will exit the shell side gas in line 459 to the added cooling heat exchanger 150, then join with the exhaust from valve 451, and the joined flow is to the condenser 146. The flow off of the condenser 146 will pick up the exit of the auto pressure control valves 260 and 262, and then enter the boiler 145. The gas off of the shell side of the pump flash pot 149 in line 460 will go to the added cooling heat exchanger 150. The exit off of this pass will go to the condenser 146, and exit to a branch off to a check valve 263 and to an auto pressure control valve 262. Check valve 263 will take a small flow during startup to the turbine exhaust header but when the turbine exhaust pressure goes above the flash pot pressure, an auto pressure control valve 262 will move the gas to a low pressure line. Normal operation is check valve 263 closed and pressure control valve 262 is controlling. Now the low pressure line off the three flash pots 147, 148, and 149 will go to the boiler 145, then to the oxygen cooler 144, and then to auto pressure control valve 264.

The four turbine exhaust flow at point 450 from FIG. 5, discussed in greater detail below, will go thru the turbine exhaust phase separator 151, and the gas off the top of the separator 151 will go into the condenser 146, while all of the liquid of the phase separator 151 will go to the three flash pots 147, 148, and 149 and the over flow valve 451. Upon the gas stream off of the turbine exhaust phase separator 151 exiting the condenser 146, during a startup mode of operation, this gas stream will pick up the exit of the two check valves 261 and 263, but during normal operation the pressure of the exhaust of the turbines will be much higher and close both check valves 261 and 263. The flow of gas from the condenser 146 will enter the boiler 145, and at the exit of the boiler 145 the gas will enter the oxygen cooler 144. The exit of the oxygen cooler 144 is to a pressure control valve 455.

The pressure control valve 264 should run wide open if all the flow from the low pressure nitrogen inlet line (FIG. 3b, line 257) can enter the liquefier. The flows from valve 264 and from FIG. 3b, line 257 will join, and go to the turbines (FIG. 5, point 265). This joined gas nitrogen flow will also join the flow from surge control check valve 272 (FIG. 5), then pass through the flow meter 270. The flow meter 270 is needed to predict a surge on the first booster 155. The booster 155 will draw in the nitrogen gas and compress the gas. The compressed gas will pick up the heat of compression and will exit to the aftercooler 156, which is a double air cooling fan system. Each fan in an embodiment is a 25-horse power belt driven fan, one is a fixed pitch fan, and the other is a variable pitch fan. The aftercooler 156 is set to hold a 90 degree temperature on the compressed nitrogen gas exit.

The nitrogen gas exit from the aftercooler 156 will branch off to three places, namely, a flow to the surge control return gas flow through control valve 271, a flow 273 to warm the preheater 152 (FIG. 4), and a flow to the next booster 159 through check valve 276. The flow through the auto surge control valve 271 will open if the math surge curve is approached. If the surge control system is called into action, then valve 271 will slowly open and the check valve 272 will open, and the flow to the booster 155 will increase. The surge control system is normally not active, but is used on startup. The next flow is to the preheater 152 at point 273 (FIG. 4). The pass through the preheater 152 is normally a small flow to keep the line active, but if the system is upset due to a failure of a nitrogen pump 169 or 170, the boiler 145 liquid will flash to gas, and the excess cold gas to the turbines will cause the turbines 153, 157, 161, and 165 to produce liquid across the blades, and the turbines will all fail. The control valve 274 (FIG. 4) is a temperature controller set to hold the flow in line 288 (FIG. 5) to about −155 degrees. The exit of flow from auto control valve 274 through the preheater 152 to line 275 (FIG. 4) is a very small flow now moved to line 275 in FIG. 5.

The last flow from the aftercooler 156 is to the check valve 276 heading to the next booster 159. The exit of the check valve 276 is joined with a small flow in from line 275 (from FIG. 4) that is a cold gas. The small flow of cold gas from line 275 will not move the inlet temperature to the booster 159 by even one degree during normal running. The gas of the check valve 276 will also be joined by the flow from surge control check valve 276 if the surge control system is active. All of the joined flows will enter the flow meter 277. The flow from flow meter 277 enters the booster 159. The exit of the booster will enter the aftercooler 160 (having the same design and operation as the aftercooler 156). Out of the aftercooler 160 the flow will branch to the auto surge control valve 278 and check valve 279 (having the same design and operation as the surge system 271), and the line to the flow meter 280.

The flow from the surge control system 282 check valve and the flow from the aftercooler 160 will enter the flow meter 280. The gas will be compressed by the next booster 163 and exit to the aftercooler 164. The exit of the aftercooler 164 will branch off to the surge control valve 281 and to the booster 167. The surge control system is normally closed, but for startup valve 281 slowly opens to a check valve 282 which will add flow to the booster 163 inlet.

The rest of the exit flow from aftercooler 164 will go to a joined flow of the surge control system exit check valve 285 and from line 458 from FIG. 4. All the flow is metered by flow sensor 283 used to predict the booster 167 surge. The flow is now called the major flow. In the booster 167 the gas will go up in pressure and temperature. The temperature will be controlled by an aftercooler 168 to hold the temperature at about 90 degrees. The exit of the aftercooler 168 flow will split to the surge control system 284. The surge control system 284 should be closed on normal operation, but on start up the valve 284 is slowly opened and that gas will move through check valve 285 to the booster 167 inlet. The flow that was not used by the surge controller system will exit to in line 500 to FIG. 4 as the major flow.

FIG. 7 THE BACKUP GAS NITROGEN SYSTEM. Referring now to FIG. 7, the backup gas nitrogen system is shown, which includes a liquid nitrogen storage tank 174 having its own venting system 46. The liquid nitrogen will move from storage tank 174 into the tube side of evaporators 178 where the liquid nitrogen is changed into a gas nitrogen. At the exit of the evaporators 178 there is a pressure regulator 45. If the purge nitrogen header should fall below its normal running pressure, then the regulator 45 will open, but otherwise the regulator 45 is closed.

There is an air feed 2 coming from the air separation unit in FIG. 1 to the back up gas nitrogen system in FIG. 7, which is to the instrument air supply. In FIG. 1, valve 112 is an open and closed valve feeding air to the auto control valves to open and close the valves the computer is controlling. This flow has above 78 psig of air pressure. Check valve 19 (FIG. 7) is provided on air feed 2 to stop a back flow of air. The exit of the check valve 19 will enter the selector 20 which will allow the air to pass during normal operation to the instrument air system 21. If the instrument air supply falls to a lower pressure then the set point, pressure regulator 30 will take over. Back flow is stopped by check valve 31.

The gas nitrogen supply coming in to the back up gas nitrogen system from FIG. 3c, line 33 can supply all the purge and instrument nitrogen for the whole plant. After the gas nitrogen is supplied, there is a check valve 32 (FIG. 7) to protect the pure nitrogen. If instrument air supply point 2 is not up to set point pressure then the check valve 31 will open and the pressure regulator 30 will now supply the instruments nitrogen needed, this will open to point 21. The main purge header, shown by the line extending vertically in FIG. 7, will wrap around the whole plant site with a two inch line. The purge header has many branch offs which are also illustrated in FIG. 7. The main supply to the purge header is the feed off of line 33, FIG. 3c, and if this is not up to pressure then regulator 45 off of the backup tank 174 will supply the nitrogen gas to the purge header.

The purpose of each of the branches off of the main purge header will now be explained. As shown in FIG. 7, there is a branch to FIG. 8, point 44 off of the purge header which provides a nitrogen supply to the oxygen filter house. As shown in FIG. 8, the main flow is to the warming nitrogen flow through flow meter 60, to open or close auto valve 61, to check valve 62, to service the filters 175 and 176 as needed. There is also a branch flow from point 44 off to provide a nitrogen purge flow to the oxygen filter box at point 47.

There are four separate branches 34, 35, 42, and 43 off of the main purge header to the turbine package shown in FIG. 5. The branch off at point 34 is providing a sealing gas supply in line 75 to turbine 153 and in line 76 to turbine 157. The branch off at point 35 is similarly supplying a sealing gas supply in line 77 to turbine 161, and in line 78 to turbine 165. The branch off at point 42 is supplying the turbine case purge, and the branch off at point 43 is supplying the oil accumulator.

Another flow off of the main purge header is to point 41 in FIG. 4, which is to the liquefier cold box purge. The flow off of point 40 to FIG. 1 is to the cold box purge. The flow off of point 39 to FIG. 1 is to a warming purge flow to the low pressure column relief valve 213 and burst disk 212. The flow off of point 38 is a purge flow of warm gas to defrost the backup storage tank vent valve (46). Finally, the flow off of points 36 and 37 goes to FIG. 2. The flow off of point 36 is to regenerate the argon drier beds, and as shown in FIG. 2 is working on argon drier bed 142, this flow will go to atmosphere 433. The flow off of point 37 will warm up the vent valve to atmosphere off of the separator 13 shown as flow 423 in FIG. 2.

THE OXYGEN FILTER HOUSE. Some air separation plant sites have built-in heat pumps and gel trap filters to remove solid concentrations in the liquid oxygen at the reboiler. Some plants have a filter to the transport trailers at the filling station. Some plants have a filter to the storage system. Those plant sites will not necessarily need the liquid oxygen filter house illustrated in FIG. 8, although the present oxygen filter house will reduce the losses and manpower needs of the existing system after the plant switches to the new liquefier of the present invention.

The inventor's new liquefier takes almost all the oxygen production out of the air separation plant as gas. This will leave behind a small amount of liquid oxygen that has some solid contamination which must be removed to hold down the concentration of the contamination. The oxygen filter house system has two gases and one liquid to move around without blending. The gasses here are pure nitrogen gas, and atmosphere air, and the liquid is pure liquid oxygen. To do this, each system must be protected. The best known way to protect a purity is to keep the pressure above atmosphere pressure, and then to use a blocking system, or a way to stop one flow from moving into the next one. Since the pressures here are above atmosphere pressure, a double block and bleed system is used. This will stop flow by a valve whose exit is to atmosphere. If a valve that is used to block a flow were to leak, then that flow could leak but only to the atmosphere, and not to the next product. All the double block and bleed nest of valves must have a relief valve.

The liquid oxygen flow from the air separation plant comes in from FIG. 1 to the oxygen filter house in FIG. 8 as a subcooled liquid, at point 302. There is a check valve 335 on the entry to the filter house, which is provided to prevent a back flow of liquid oxygen. If the liquid oxygen in line 302 is not pure enough to put to storage, or if both filters have clogged, the liquid oxygen must go somewhere. One place the liquid oxygen with a bad purity should go is to the dump. But, if the filters are being worked on and are not able to be used, then there is a bypass to allow the solids to go to storage during a short time the filters are being worked on.

If the oxygen produced by the air separation plant is to be dumped, the whole system is assumed to be or going bad. Quick action must be taken, and all the valves to be closed at once are 313, 316, 381, 61, 63, 69, 64, 70, 343, 357, 346, 360, 377, 378, 339, 372, 351, 365, 352, 366, 342, 355, and 369. In addition, all the valves to open at the same time are 68, 338, 345, 376, 359, 315, 66, 72, 341, 350, 364, 354, 368, 371, and 380. The valves to control the flows are valve 312, 68, 336, 177. Valve 312 controls the height of the tube side of the oxygen production flash pot vessel 147 (FIG. 4). Valve 68 controls the warm nitrogen flow seen at flow meter 60 to a flow of 100 scfh but will see zero flow single making the valve 68 to auto flow control to a wide open. Valve 336 controls the liquid height of the reboiler bath vessel 116 (FIG. 1). Then the vent pressure control valve 382 on the storage tank, which will hold a one psig on the storage tank. This will vent all trapped gas and liquids to a total dump to protect the storage tank from contamination.

When the purity is established, the system of opening the different subsystems starts. The largest flow will be the liquefier oxygen (from FIG. 4, point 305) to storage. On production dump the flow from the liquefier past check valve 310 to dump is controlled by valve 312. When the purity is good from the liquefier, valve 312 continues to dump while auto level control valve 313 is opened in manual mode. The flow to valve 313 just opened will vent out of the bleed valve 315. Once the liquid oxygen is at a steady flow out of bleed valve 315, valve 316 is slowly opened, while valve 315 is closed. The flow will then go out the bleed valve 380. Once the liquid flow is steady from bleed valve 380 and the purity is still good, then valve 381 to storage is opened. The amount of liquid now moving to storage and to dump will cause the auto level control valve 312 to see a lower level than the set point and begin to close. When valve 312 is about 5 percent auto open, valve 313 is put into auto level control auto mode. Auto level control valve 312 is to be set to a higher liquid level control point than valve 313, and is to be kept in auto control mode in case the flow out of the vessel 147 starts to back up so the liquid oxygen will have a place to go. The system as just described has now put liquid oxygen to storage from the liquefier.

When the purity of the air separation plant's liquid oxygen is good, then for a short time the oxygen with all the solids will go to storage during the time the filters are being worked on. The filters must be opened slowly, and dumping or bypass liquid to storage can continue. In the embodiment shown in FIG. 8, filter 175 will be set up to filter, and filter 176 will be put on reactivation. All of the valves in the filter system will be positioned as if you are going to dump with the air separation plant liquid oxygen, and going to storage with the liquefier liquid oxygen, to here. Liquid oxygen from the production plant comes in from FIG. 1, point 302 to a check valve 335 leading to a shell side reboiler level control valve 336 connected to a dump valve 338. Opening valve 342 will cause a backward flow of liquid oxygen out bleed valve 341. Once a steady flow of liquid oxygen is seen exiting bleed valve 341, then valve 339 is opened and valves 341 and 338 are closed. The system is now set up so that the production plant liquid oxygen is bypassing the filters and going to storage. Flow control is still provided from liquid level control valve 336.

Setting up filter 175 for service. The liquid oxygen is at a good purity and first open reboiler auto level controller valve 343 in manual mode is opened about 25%. This will vent liquid oxygen out bleed valve 345. When a steady stream of liquid oxygen is detected, then valve 346 is opened, and bleed valve 345 is closed. This will vent liquid oxygen out bleed valve 350. The line supplying bleed valve 350 is small and it should take a few minutes to cool down enough to allow a steady flow of liquid oxygen to exit. A close eye must be kept on the active liquid controller, as it is very possible to over draw the liquid from the reboiler, and if this is starting to happen the auto controller valve 336 will close. If the liquid from the reboiler is being overdrawn then for a short time valve 350 should be closed until the reboiler height is reestablished and the auto controller valve 336 reopens. Then, valve 350 is reopened. By monitoring the temperature sensor 348, the cooling process can be tracked. After the liquid oxygen is flowing at a steady stream out valve 350 and the purity is still satisfactory, then valve 352 is opened to vent out bleed valve 354 and valve 350 is closed. After a steady stream of liquid oxygen is seen exiting valve 354 then open valve 355 and close valve 354. The reboiler auto controller valve 336 is also then set to a higher level and reboiler auto level controller 343 is set to auto mode with a set point at normal reboiler height. The bypass line is then closed by closing valves 342 and 339, and then opening valves 338 and 341. The system is now filtering the solids out of the liquid oxygen from the air separation plant, and the liquefier liquid oxygen is joined to storage.

Next, filter 176 is reactivated, going from the same sequence as above. Recap closed valves are 61, 63, 64, 69, 70, 345, 357, 360, 377, 378, 339, 350, 351, 372, 365, 354, 366, 342, 369, 380, and 315. The valves open at this time are 338, 341, 346, 352, 355, 376, 371, 359, 364, 368, 316 and 381. The valves in auto control are 68, 313, 312, 343, 336, and 382.

Bleed valve 364 is open so any liquid could vent, but to make sure valve 61 is opened so that a flow will be started and seen by flow monitor 60. Flow monitor 60 will be set to 100 scfh and for now valve 68 will control the flow. Then flow controller valve 69 is opened in manual mode to 25% open, and the gas nitrogen will vent out of valve 72. Auto flow controller valve 68 will then start to close, because valve 69 is taking some of the flow. Then, valve 70 is opened, and valve 72 is closed. Auto control valve 68 is set to 90 scfh and auto flow controller valve 69 is adjusted to a set point of 100. If the flow falls below 90 scfh then valve 68 will be called to open. If valve 68 is called to open, then the operator will be notified. The solid contamination the filter removes will turn to gas before the filter temperature 362 hits −90 degrees Fahrenheit. When the temperature hits −80 degrees Fahrenheit the reactivation is finished. Now, valves 69, 70, and 364 are closed, and valve 72 is opened. Valve 68 is in control and set to open if the flow goes below 90 scfh as seen by flow monitor 60. Closing valve 61 therefore will stop the entry of nitrogen gas and by default valve 68 will auto open.

Moving to the cool down of filter 176, the cleaned exit flow of filter 175 is used to cool down filter 176. Opening valve 351 will vent liquid oxygen out bleed valve 371. Once a steady stream of liquid oxygen is seen exiting valve 371, valve 371 is closed, and auto flow control valve 372 is opened, and will be open 25% in manual mode. This will pass a liquid oxygen flow through a check valve (373), to a flow monitor (375), and exit valve 376. Once a steady flow of liquid oxygen is seen exiting valve 376, then valves 378 and 364 are opened. The cool down flow will be seen on flow meter 375.

Auto flow controller valve 372 will be put into auto control mode, and be set to 100 scfh controlling the flow seen at flow meter 375. The cooling process will be seen on temperature monitor 362. This process of cooling the filter will take hours due to the small flow. Once the temperature monitor 362 reaches a −250 then the cool down mode is complete, and the filter 176 will be put on standby mode.

To set up a standby mode for filter 176, the flowing valves must be closed; 351, 372, 378, 364, and the valves to be open are 371 and 376. The process of standby is to let a cooled filter 176 sit with valves closed. If there is any gas expansion, the vessel is protected by relief valve 363. In addition, there will be a cycling of opening and closing valve 364 once every ten minutes, since protecting a vessel with only a relief valve may be insufficient in reducing the expansion of gas trapped.

The next mode of operation of the liquid oxygen filters is dull filter running, which is how to move the filtration from one filter to the next. The standby mode is stopped. The only valve in operation on filter 176 is valve 364, which will open and close on a timer of once every 10 minutes for one tenth of a second. This will stop on an open sequence, and valve 357 will open in manual control to 25% open. A flow of oxygen liquid will be seen coming out of bleed valve 359. Then valve 360 is opened and valve 359 is closed. Liquid oxygen will go out through valve 364. During the startup of filter 176 the amount of liquid oxygen to be used will cause auto level control valve 343 to start closing. If valve 343 were to close, then the valve opening on auto level control valve 357 which is in manual mode is reduced to 10%. After liquid oxygen is exiting valve 364 then valve 366 is opened, and bleed valve 364 is closed. Liquid oxygen will flow out of bleed valve 368. After that valve 369 is opened. Now both filters 175 and 176 are filtering.

The next step is to stop filter 175. Level controller valve 343 in manual is set at 5% open, and level controller valve 357 is put into auto mode with a set point of the reboiler height. This will take about 3 to 5 minutes to settle out, and then valves 343, 346, 351, 352, and 355 are closed, and valves 354, 350, and 354 are opened.

Filter 175 is drained, with any liquid oxygen in filter 175 will drain out of valve 350 as the liquid turns to gas. In addition, valve 61 is opened and auto control valve 63 is set to 100 scfh. This will vent nitrogen gas out of valve 66. Then valve 64 is opened and valve 66 is closed. Auto flow control valve 68 is set to open below 90 scfh, and auto control valve 63 is set to open below 100 scfh. This should cause valve 68 to close because the flow will be above the set point. The liquid in filter 175 will be draining out of valve 350.

Filter 175 is put in to heat up, after the liquid is drained out of valve 350. Then the flow will stay the same. The point to monitor is the filter temperature sensor 348. When the filter temperature hits −80 degrees Fahrenheit, the heat up is done.

To put filter 175 into cool down, the heat up is stopped by closing valves 61 and 63. This will cause auto flow control valve 68 to open due to a loss of flow. The set point for valve 68 is open below 90 scfh. Valve 64 is then closed, and bleed valve 66 is opened. Using the clean liquid oxygen out of filter 176, valve 365 is opened to bleed valve 371 is closed. After valve 371 has a steady flow of liquid oxygen exiting it, then valve 372 opened and valve 371 is closed. Valve 372 is put in manual mode and open 10%, and once liquid oxygen comes out of valve 376, open valve 377 and close valve 376. Flow meter 375 will show a flow and should be set to a flow rate of 100 scfh and auto flow control valve 372 will be used to control the flow. The flow will exit valve 350. Once the flow cools down the filter to −250 as seen on temperature sensor 348 then the cool down is done.

Put filter 175 to stand by mode. Stop cool down and close valves 365, 372, 377, and 350. Open bleed valves 371, and 376. Now cycle valve 350 open and closed once every ten minutes to stop an over pressure.

Put filter 175 into dull operation mode. When needed filter 175 will be put into dull operation with filter 176. First open auto level control valve 343 in manual mode at ten percent open. This will vent liquid oxygen out of bleed valve 345. When a steady flow of liquid oxygen exits bleed valve 345, then open valve 346, and close bleed valve 345. The flow will exit valve open valve 350. The temperature monitor 348 will show the progression of cool down to operation. Once the flow out of valve 350 shows a steady stream of liquid oxygen then open valve 352 and close valve 350. The flow will now exit bleed valve 354. Once bleed valve 354 shows a steady flow of liquid oxygen then open valve 355, and close valve 354. Now put auto level controller valve 343 into auto mode and set auto level controller valve 357 into manual mode at five percent open. Once the system is working for a few minutes and is stable, then put the filter 176 into stop mode. Put valve 357 into auto level control.

Put filter 176 into a stop mode. The system just switched over from filter 176 on line to filter 175 on line. Now stop filter 176 and close all valves 357, 360, 366, and 369. Now open 368, 364, and 359. Any liquid in filter 176 will be able to drain out of valve 364. Then again go through the warm up steps above.

During the operation of the filters there is a differential pressure gauge to show filter clogging. This should be monitored and logged to find out how long the filter can be in operation. The differential pressure gauge for filter 175 is 347, and the filter 176 has differential pressure gauge 361. This is a list of relief valves found on FIG. 8. On the liquid oxygen from the liquefier to the filter house is relief valve 311 to protect the line if valves 312, 313, and check valve 310 closed with liquid oxygen trapped and changing state to a gas. Relief valve 314 is there to protect the line if valves 313, 315, and 316 closed with liquid oxygen trapped and changing state to a gas. Relief valve 340 is there to protect the line if valves 339, 342, and 341 closed with liquid oxygen trapped and changing state to a gas. Relief valve 349 is there to protect the line and filter 175 if valves 352, 351, 350, 64, 346, and 377 closed with liquid oxygen trapped and changing state to a gas. Relief valve 370 is there to protect the line if valves 371, 351, 365, and 372 closed with liquid oxygen trapped and changing state to a gas. Relief valve 374 is there to protect the line if valves 372, check valve 373, 378, 376, and 377 closed with liquid oxygen trapped and changing state to a gas. Relief valve 344 is there to protect the line if valves 343, 354, and 346 closed with liquid oxygen trapped and changing state to a gas. Relief valve 358 is there to protect the line if valves 360, 357 and 359 closed with liquid oxygen trapped and changing state to a gas. Relief valve 356 is there to protect the line if valves 357, 343, 336, and check valve 335 closed with liquid oxygen trapped and changing state to a gas. Relief valve 67 is there to protect the line if valves 69, 68, check valve 62, and 63 closed with liquid oxygen trapped and changing state to a gas. Relief valve 71 is there to protect the line if valves 72, 70, and 69 closed with liquid oxygen trapped and changing state to a gas. Relief valve 363 is there to protect the filter 176 and the lines if valves 366, 365, 364, 70, 360, and 378 closed with liquid oxygen trapped and changing state to a gas. Relief valve 367 is there to protect the line if valves 366, 368, and 369 closed with liquid oxygen trapped and changing state to a gas. Relief valve 379 is there to protect the line if valves 381, 380, 342, 355, 369, and 316 closed with liquid oxygen trapped and changing state to a gas. Relief valve 353 is there to protect the line if valves 352, 354, and 355 closed with liquid oxygen trapped and changing state to a gas. Relief valve 65 is there to protect the line if valves 63, 64, and 66 closed with liquid oxygen trapped and changing state to a gas. Relief valve 337 is there to protect the line if valves 336, 338, and 339 closed with liquid oxygen trapped and changing state to a gas.

TABLE

Temperature
Pressure
Flow
Ref.
Location

(Fahrenheit)
(psig)
(scfh)
No.
(FIG. No.)
Notes

ref
ref
ref
ref
ref
all of the nitrogen that

enters the liquefier

45.10
78.44
15500.000000
2
FIG. 1&7
instrument air removal

(psig). To FIG. 2

45.1
78.44
15500.000000
2
FIG. 7&1
Instrument air feed just

after MS's filters FIG. 1

43.93
77.09
780000.000000
3
FIG. 1
warm side MHE (psig)

point 113

−277.12
73.17
780000.000000
4
FIG. 1
exit MHE 113 enter

HPC 114 (psig)

−275.94
73.44
437000.000000
5
FIG. 1
Liquid at the bottom of

the HPC 114 (psig)

−280.00
51.50
437000.000000
6
FIG. 1
HPC 114 bottom liquid

raised 55′ now entering

the SC 117 (psig)

−292.00
48.61
437000.000000
7
FIG. 1
HPC 114 bottom liquid

exiting the SC 117

(psig)

−305.00
35.00
437000.000000
8
FIG. 1
Raised 45′ split to

control valves feeding

POINTS 9 & 10. (psig)

−308.00
23.61
252000.000000
9
FIG. 1
Liquid into POINT 120,

shell side (psia)

−309.28
18.83
185000.000000
10
FIG. 1
From POINT 114 bottom

liquid after control

valve into the POINT

116 tray 44, (psia)

−307.80
26.11
2000.000000
11
FIG. 1
liquid exiting the point

120 to its control valve

(psia)

−308.51
18.97
2000.000000
12
FIG. 1
liquid from the POINT

120 after the control

valve now entering the

POINT 116 tray 42

(psia)

−307.00
20.50
250000.000000
13
FIG. 1
gas exit the POINT 120

to a control valve. (psia)

−308.90
18.90
250000.000000
14
FIG. 1
Gas from the POINT120

control valve to POINT

116 to tray 43 (psia)

−301.55
20.27
206300.000000
15
FIG. 1
LPC 114 tray 24 gas to

CRA 118 (psia)

−300.00
23.27
199013.839220
16
FIG. 1
liquid exit CRA 118

(psia)

−301.55
20.27
199013.839220
17
FIG. 1
liquid from CRA 118 after

the control valve to

LPC 116 tray 24 (psia)

80
78.42
15500.000000
19
FIG. 7
check valve to the

instruments

80
78.4
15500.000000
20
FIG. 7
all the gas needed to run

the instruments system.

normally air.

80
78.38
15500.000000
21
FIG. 7
Feeds auto valves

80
66.93
0.000000
30
FIG. 7
instrument nitrogen to

instrument air pressure

regulator

80
65
0.000000
31
FIG. 7
backup nitrogen check

valve

80
66.95
16810.000000
32
FIG. 7
check valve inlet gas

nitrogen to purge system

37.00
66.97
16810.000000
33
FIG. 3&7
Nitrogen from valve 238

to FIG. 7 the nitrogen to

purge system

37.00
66.97
16810.000000
33
FIG. 7&3
from FIG. 3

80.00
65.00
4000
34
FIG. 5&7
Seal gas from FIG. 7 to

feed points 75 and 76

80
65
4000.000000
34
FIG. 7&5
Seal gas to turbines on

FIG. 5

80.00
65.00
4000
35
FIG. 5&7
Seal gas from FIG. 7 to

feed points 77 and 78

80
65
4000.000000
35
FIG. 7&5
Seal gas to turbines

FIG. 5

80.00
65.00
6500.000000
36
FIG. 2
pure nitrogen gas from

FIG. 7 to argon dryer

bed on reactivation.

80
65
6500.000000
36
FIG. 7&2
Argon drier regeneration

FIG. 2

80.00
15.00
200.000000
37
FIG. 2&7
nitrogen gas purge flow

to warm up vent valve

for 423 flow.

80
65
200.000000
37
FIG. 7&2
Warming purge to the

refined argon separator

nitrogen vent valve FIG. 2

80
65
200.000000
38
FIG. 7
Warming purge to the

instrument nitrogen back

up tank 174 vent valve

80.00
65.00
200.000000
39
FIG. 1
from FIG. 7 gas nitrogen

to warm the burst disk

and relief valve

80
65
200.000000
39
FIG. 7&1
Warming purge for low

pressure column vent

and relieve valve FIG. 1

80.00
65.00
800.000000
40
FIG. 1&7
this is a nitrogen gas to

purge the cold box coming

from FIG. 7

80
65
800.000000
40
FIG. 7&1
Cold box casing purge

FIG. 1

80.00
65.00
200.000000
41
FIG. 4&7
nitrogen purge flow from

FIG. 7 to liquefier box

purge

80
65
200.000000
41
FIG. 7&4
Liquefier casing purge

FIG. 4

80.00
65.00
400.000000
42
FIG. 5&7
FIG. 5 turbine duct casing

purge from FIG. 7

80
65
400.000000
42
FIG. 7&5
Turbine duct casing

purge FIG. 5

80.00
65.00
10.000000
43
FIG. 5&7
FIG. 5 nitrogen pressure

to the oil accumulator

from FIG. 7

80
65
10.000000
43
FIG. 7&5
to FIG. 5 turbine oil

accumulator

80
65
300.000000
44
FIG. 7&8
To oxygen filters, warming

nitrogen purge and

case purge FIG. 8 point

44

80.00
65.00
300.000000
44
FIG. 8&7
from FIG. 7, warming

nitrogen and purge inlet

psig

80
60
0.000000
45
FIG. 7
purge backup pressure

regulator

80
125
0.000000
46
FIG. 7
Back up nitrogen tank

174 vent

80.00
65.00
200.000000
47
FIG. 8
oxygen filter case purge

FIG. 8 psig

−311.60
18.39
37900.000000
50
FIG. 1
waste nitrogen from tray

10 from point 116 LPC

to SC 117

−282.00
17.64
37900.000000
51
FIG. 1
waste nitrogen from SC

117 to MHE 113 (psia)

37.00
16.50
37900.000000
52
FIG. 1
Waste nitrogen exit

MHE 113 to a flow control

valve then MS bed (psia)

37.00
15.90
37900.000000
53
FIG. 1
waste nitrogen flow, after

control valve to the

MS reactivation heater

122 (psia)

37.00
15.90
37900.000000
54
FIG. 1
hot or cold waste nitrogen

to mol sieve bed on

reactivation

80.00
14.70
37900.000000
55
FIG. 1
waste nitrogen to vent

after the mol sieve on

reactivation

80.00
65.00
100.000000
60
FIG. 8
warming nitrogen inlet

flow meter psig

80.00
65.00
100.000000
61
FIG. 8
auto valve for warming

nitrogen inlet psig

80.00
64.99
100.000000
62
FIG. 8
warming nitrogen inlet

flow check valve psig

80.00
64.98
0.000000
63
FIG. 8
warming nitrogen auto

valve to filter number

175 psig

−298.00
23.92
0.000000
64
FIG. 8
shut off valve for warming

nitrogen on filter

number 175 psia

80.00
14.70
0.000000
65
FIG. 8
warming nitrogen relief

valve psia

80.00
14.70
0.000000
66
FIG. 8
warming nitrogen auto

double block and bleed

vent psia

80.00
64.98
0.000000
67
FIG. 8
warming nitrogen header

relief valve psig

80.00
64.98
0.000000
68
FIG. 8
warming nitrogen header

vent psig

80.00
64.97
100.000000
69
FIG. 8
warming nitrogen auto

valve to filter number

176, psig

80.00
64.96
100.000000
70
FIG. 8
shut off valve for warming

nitrogen on filter

number 176, psig

80.00
64.96
0.000000
71
FIG. 8
warming nitrogen relief

valve psig

80.00
64.96
0.000000
72
FIG. 8
warming nitrogen auto

double block and bleed

vent psig

80.00
65.00
2,000.000000
75
FIG. 5
Nitrogen gas from point

34 for seal gas to turbine

153

blank
blank
2,000.000000
76
FIG. 5
Nitrogen gas from point

34 for seal gas to turbine

157

80.00
65.00
2,000.000000
77
FIG. 5
Nitrogen gas from point

35 for seal gas to turbine

161

blank
blank
2,000.000000
78
FIG. 5
Nitrogen gas from point

35 for seal gas to turbine

165

72.81
14.50
795754.864039
100
FIG. 1
Air separation filter

house 795,754.8 scfh air

flow (psia)

168.00
85.51
795754.738708
101
FIG. 1
exit the 4th stage (psig)

168.00
60.00
0.125331
102
FIG. 1
The three intercoolers

condensation will strip

away this. The solubility

of this gas in the first

waters. (psig)

168.00
85.51
0.000000
103
FIG. 1
MAC VENT (psig)

90.00
83.31
795754.738708
104
FIG. 1
exit aftercooler (psig)

38.00
82.81
795754.738708
105
FIG. 1
chiller unit exit

38.00
82.31
795746.763479
106
FIG. 1
chilled air out of the

water separator (psig)

38.00
82.81
7.975229
107
FIG. 1
water separator water

blow down (psig)

50.00
80.51
246.763478
108
FIG. 1
molecular sieve beds and

dust filter removes this

(psig)

vessel
vessel
vessel
109
FIG. 1
second mol sieve vessel

45.47
78.51
795500.000000
110
FIG. 1
the exit of the dust filter

(psig)

44.74
77.24
780000.000000
111
FIG. 1
Main flow meter (psig)

45.10
78.44
15500.000000
112
FIG. 1
open or closed valve to

instrument air system

vessel
vessel
0.000000
113
FIG. 1
the main heat exchanger

five pass heat exchanger

vessel
vessel
vessel
114
FIG. 1
vessel the high pressure

column

vessel
vessel
vessel
115
FIG. 1
this is the high pressure

reboiler in the low

pressure column

vessel
vessel
0.000000
116
FIG. 1
vessel the low pressure

column

vessel
vessel
0.000000
117
FIG. 1
the sub cooler, five pass

heat exchanger

vessel
vessel
vessel
118
FIG. 1
vessel the crude argon

column

vessel
vessel
vessel
119
FIG. 1
this is the crude argon

column reboiler in the

argon condenser

vessel
vessel
0.000000
120
FIG. 1
Vessel the crude argon

condenser, two pass heat

exchanger, phase exchanger

vessel
vessel
0.000000
121
FIG. 1
Vessel the crude argon

phase separator

heater
heater
heater
122
FIG. 1
heater for mol sieve

−295.00
20.00
38670.824876
123
FIG. 2
REF ARGON

TRANSPORT

TRAILER

−295.00
20.00
1299339.715842
124
FIG. 2
REF ARGON

STORAGE TANK

heat
heat
heat
125
FIG. 2
argon recondenser

exchanger
exchanger
exchanger

exchanger side

liquid
liquid
0.000000
126
FIG. 2
argon recondenser liquid

holder
holder

nitrogen side

hydrogen
hydrogen
hydrogen
127
FIG. 2
ARGON HYGROGEN

separator
separator
separator

SEPERATOR

−297.00
26.00
14191.128395
128
FIG. 2
argon reboiler tube side

−297.00
26.00
7095.564197
129
FIG. 2
outer shell holding liquid

argon

vessel
vessel
0.000000
130
FIG. 2
ARGON PURE

COLUMN

heat
heat
0.000000
131
FIG. 2
pure argon condenser

exchanger
exchanger

heat exchanger

−307.00
24.70
7587.889152
132
FIG. 2
pure argon phase

separator

heat
heat
heat
133
FIG. 2
crude and combusted

exchanger
exchanger
exchanger

argon heat exchanger

98.00
15.00
7491.413203
134
FIG. 2
argon compressor

98.00
56.90
7491.413203
135
FIG. 2
argon compressor after-

cooler

80.00
3500.00
240000.000000
136
FIG. 2
hydrogen tube trailer

88.00
56.00
7844.826016
137
FIG. 2
argon flame arrester

87.00
56.00
7844.826016
138
FIG. 2
oxygen and hydrogen

catalyst bed

heat
heat
0.000000
139
FIG. 2
deoxo water cooled

exchanger
exchanger

aftercooler

heat
heat
0.000000
140
FIG. 2
combusted argon water

exchanger
exchanger

phase separator

95.00
55.00
7368.313118
141
FIG. 2
one of two dryer vessels

this one is on line

80.00
65.00
6500.000000
142
FIG. 2
one of two dryer vessels

this one is on

reactivation

vessel
vessel
vessel
143
FIG. 2
argon dust filter

heat
heat
heat
144
FIG. 4
Four pass heat exchanger

exchanger
exchanger
exchanger

called the oxygen cooler

heat
heat
heat
145
FIG. 4
Five pass heat exchanger

exchanger
exchanger
exchanger

called the boiler

heat
heat
heat
146
FIG. 4
Six pass heat exchanger

exchanger
exchanger
exchanger

called the condenser

flash
flash
flash
147
FIG. 4
Shell and tube heat ex-

pot
pot
pot

changer called the oxy-

gen production flash pot

flash
flash
flash
148
FIG. 4
Shell and tube heat ex-

pot
pot
pot

changer called the nitro-

gen production flash pot

flash
flash
flash
149
FIG. 4
Shell and tube heat ex-

pot
pot
pot

changer called the nitro-

gen pump flash pot

heat
heat
heat
150
FIG. 4
Three pass heat ex-

exchanger
exchanger
exchanger

changer called the added

cooling heat exchanger

phase
phase
phase
151
FIG. 4
Exhaust of the turbines

separator
separator
separator

phase separator

heat
heat
heat
152
FIG. 4
Four pass heat exchanger

exchanger
exchanger
exchanger

called the per heater

−155.00
420.00
180,000.000000
153
FIG. 5
turbine expander inlet

−287.00
84.00
180,000.000000
153
FIG. 5
turbine expander outlet

guide
guide
guide
154
FIG. 5
inlet guide vanes

vanes
vanes
vanes

55.00
14.90
398,184.701923
155
FIG. 5
155 turbine booster inlet

245.00
26.74
398,184.701923
155
FIG. 5
155 turbine booster

outlet

245.00
26.74
398,184.701923
156
FIG. 5
156 turbine after cooler

inlet

90.00
25.74
398,184.701923
156
FIG. 5
156 turbine after cooler

outlet

−155.00
420.00
180,000.000000
157
FIG. 5
turbine expander inlet

−287.00
84.00
180,000.000000
157
FIG. 5
turbine expander outlet

guide
guide
guide
158
FIG. 5
inlet guide vanes

vanes
vanes
vanes

87.00
25.74
398,184.701923
159
FIG. 5
inlet to turbine 159

255.00
42.32
398,184.701923
159
FIG. 5
outlet of turbine 159 to

aftercooler

255.00
42.32
398,184.701923
160
FIG. 5
into aftercooler 160

90.00
41.32
398,184.701923
160
FIG. 5
exit of 160 aftercooler

−155.00
420.00
180,000.000000
161
FIG. 5
turbine expander inlet

−287.00
84.00
180,000.000000
161
FIG. 5
turbine expander outlet

guide
guide
guide
162
FIG. 5
inlet guide vanes

vanes
vanes
vanes

90.00
41.32
398,184.701923
163
FIG. 5
flow into turbine booster

163

265.00
66.52
398,184.701923
163
FIG. 5
flow out of 163

265.00
66.52
398,184.701923
164
FIG. 5
turbine booster after

cooler 164 inlet

90.00
65.52
398,184.701923
164
FIG. 5
turbine booster after

cooler 164 outlet

−155.00
420.00
360,000.000000
165
FIG. 5
turbine expander inlet

−287.00
84.00
360,000.000000
165
FIG. 5
turbine expander outlet

guide
guide
guide
166
FIG. 5
inlet guide vanes

vanes
vanes
vanes

50.00
65.00
1,465,374.701923
167
FIG. 5
flow into turbine booster

167

250.00
112.82
1,465,374.701923
167
FIG. 5
flow out of turbine

booster 167

250.00
112.82
1,465,374.701923
168
FIG. 5
flow into turbine booster

after cooler 168

90.00
111.82
1,465,374.701923
168
FIG. 5
flow out of turbine

booster after cooler 168

pump
pump
pump
169
FIG. 6
liquid nitrogen pump

pump
pump
pump
170
FIG. 6
liquid nitrogen pump

−320.00
1.00
0.000000
171
FIG. 6
LIQUID NITROGEN

STORAGE TANK

80.00
14.70
0.000000
172
FIG. 6
NITROGEN TANK

PUMP BACK PUMP

−280
120
1163160.000000
174
FIG. 7
NBT Backup liquid

nitrogen storage tank

HOLD 36 HOURS

filter
filter
filter
175
FIG. 8
oxygen filter number 1

filter
filter
filter
176
FIG. 8
oxygen filter number 2

tank
tank
tank
177
FIG. 8
oxygen storage tank

80
80
0.000000
178
FIG. 7
tube side nitrogen

evaporators

−290.89
70.00
841180.060000
200
FIG. 1
total gas exiting the top

of the HPC 114 (psig)

−290.89
70.00
630180.060000
201
FIG. 1
nitrogen gas split off of

200 going to the reboiler

115. (psig)

−290.89
70.00
211000.000000
202
FIG. 1
this is the gas at the top

of the HPC 114 that is

removed to the entry

MHE 113 cold side

(psig)

37.00
67.00
211000.000000
203
FIG. 1&3
high pressure nitrogen

off of MHE 113 warm

side. (psig) to FIG. 3

37.00
67.00
211000.000000
203
FIG. 3&1
From 113 MHE high

pressure column gas

nitrogen from FIG. 1

controlled by the ASU

−317.40
17.31
362637.548954
210
FIG. 1
top of the LPC 116 pure

nitrogen gas exit (psia)

80.00
17.30
0.000000
211
FIG. 1
Low pressure column

common line to a burst

disk and a relief valve

80.00
14.70
0.000000
212
FIG. 1
burst disk to protect the

low pressure column

80.00
14.70
0.000000
213
FIG. 1
relief valve to protect the

low pressure column

−317.40
17.31
371184.701923
214
FIG. 1
Low pressure nitrogen

blended flow to the SC

117 (psia).

−282.00
17.10
371184.701923
215
FIG. 1
combined pure nitrogen

low pressures exit the

SC 117 to MHE 113

cold side (psia)

37.29
14.94
371184.701923
216
FIG. 1&3
exit of MHE 113 low

pressure pure nitrogen

gas to FIG. 3 (psia)

37.29
14.94
371184.701923
216
FIG. 3&1
Low pressure nitrogen

flow from 113 MHE

FIG. 1

−292.59
75.97
630180.060000
220
FIG. 1
liquid nitrogen removed

from the POINT 115 re-

boiler. (psig)

−292.59
75.97
498180.060000
221
FIG. 1
liquid to the top tray #38

of the POINT 114, cold

cap. (psig)

−292.59
75.97
132000.000000
222
FIG. 1
Pure liquid nitrogen

from POINT 115 to the

POINT 117 subcooler.

(psig)

−303.00
54.10
132000.000000
223
FIG. 1
The POINT 115 pure

liquid nitrogen exit SC

117 raise 45′ to auto

control valve. (psig)

−317.40
17.31
132000.000000
224
FIG. 1
liquid nitrogen out

control valve (psia)

−317.40
17.31
134345.000000
225
FIG. 1
combined liquid nitrogen

to LPC 116 (psia)

37.00
66.99
211000.000000
231
FIG. 3
High pressure column

gas nitrogen flow meter

flow set by ASU

37.00
66.99
211000.000000
232
FIG. 3
inlet to liquefier auto

valve

37.00
66.98
0.000000
233
FIG. 3
High pressure column

gas nitrogen over load

flow meter

37.00
14.70
0.000000
234
FIG. 3
relief valve EXIT

37.00
14.70
0.000000
235
FIG. 3
over load auto vent valve

EXIT

37.00
66.98
211000.000000
236
FIG. 3
inlet to liquefier check

valve

37.00
66.97
211000.000000
237
FIG. 3
inlet flow meter to

liquefier high pressure

column gas nitrogen and

purge system

37.00
66.97
16810.000000
238
FIG. 3
Open or closed valve,

for the nitrogen purge

system

37.00
66.96
194190.000000
239
FIG. 3&4
High pressure column

gas nitrogen to FIG. 4

the liquefier

37.00
66.96
194190.000000
239
FIG. 4&3
higher pressure from

FIG. 3 point 239

37.29
14.93
371184.701923
250
FIG. 3
low pressure nitrogen

flow meter set by ASU

37.29
14.93
371184.701923
251
FIG. 3
inlet to liquefier auto

flow control valve

37.29
14.93
0.000000
252
FIG. 3
Low pressure nitrogen

over load flow meter

37.29
14.93
0.000000
253
FIG. 3
relief valve EXIT

37.29
14.93
0.000000
254
FIG. 3
over load auto vent valve

EXIT

37.29
14.93
371184.701923
255
FIG. 3
inlet to liquefier check

valve

37.29
14.93
371184.701923
256
FIG. 3
Into liquefier low

pressure gas nitrogen

flow meter

37.29
14.93
371184.701923
257
FIG. 3&4
low pressure gas nitrogen

inlet to liquefier to

FIG. 4

37.29
14.93
371184.701923
257
FIG. 4&3
low pressure nitrogen

gas from inlet or vent

FIG. 3 point 257

−255.00
17.00
5000.000000
260
FIG. 4
low pressure nitrogen

gas through 260 from

147 shell side

−255.00
17.00
0.000000
261
FIG. 4
low pressure nitrogen

gas through 261 = zero

due to low pressure

−255.00
17.00
15000.000000
262
FIG. 4
low pressure nitrogen

gas through 262 from

149 shell side

−255.00
17.00
0.000000
263
FIG. 4
low pressure nitrogen

gas through 263 = zero

due to low pressure

50.00
15.00
27000.000000
264
FIG. 4
lower pressure gas

nitrogen through 145

boiler then to 144

oxygen cooler then

through valve 264

45.00
14.90
398184.701923
265
FIG. 4&5
all low pressure gas

nitrogen to FIG. 5 point

265

55.00
14.90
398,184.701923
265
FIG. 5&4
From FIG. 4 low pressure

nitrogen feed to 270

55.00
14.90
398,184.701923
270
FIG. 5
155 booster inlet flow

controller

80.00
25.74
0.000000
271
FIG. 5
155 turbine surge

controller inlet

80.00
14.90
0.000000
271
FIG. 5
155 turbine surge

controller outlet

80.00
14.90
0.000000
272
FIG. 5
155 turbine surge check

valve outlet

80.00
14.90
0.000000
272
FIG. 5
155 turbine surge check

valve inlet

90.00
25.74
1000.000000
273
FIG. 4&5
hot gas from 156 FIG. 5

to here

90.00
25.74
1,000.000000
273
FIG. 5&4
hot gas from 156 outlet

to FIG. 4, 274 control

valve

90.00
25.74
1000.000000
274
FIG. 4
Control valve hot gas

into 152

−260.00
25.74
1000.000000
275
FIG. 4&5
cooler gas exit 152 to

FIG. 5

−240.00
25.74
1,000.000000
275
FIG. 5&4
from FIG. 4 exit of 152,

to here after check valve

276.

88.00
25.74
397,184.701923
276
FIG. 5
flow into 276 check

valve.

88.00
25.74
397,184.701923
276
FIG. 5
Flow from 276, to turbine

flow controller 277

87.00
25.74
398,184.701923
277
FIG. 5
flow controller 277,

booster inlet 159

80.00
41.32
0.000000
278
FIG. 5
inlet to 159 surge

controller

80.00
25.74
0.000000
278
FIG. 5
outlet of 159 surge

controller

80.00
25.74
0.000000
279
FIG. 5
flow exit check valve

279 surge control inlet to

159

90.00
41.32
398,184.701923
280
FIG. 5
flow through flow

controller 280

90.00
65.52
0.000000
281
FIG. 5
turbine booster surge

controller inlet 281

80.00
41.32
0.000000
281
FIG. 5
turbine booster surge

controller 281 exit.

80.00
41.32
0.000000
282
FIG. 5
exit of the surge check

valve 282

80.00
41.32
0.000000
282
FIG. 5
turbine booster surge

check valve 282 inlet

50.00
65.00
1,465,374.701923
283
FIG. 5
flow through flow

controller 283 START

MAJOR FLOW

90.00
111.82
0.000000
284
FIG. 5
turbine booster surge

controller 284 inlet.

80.00
65.00
0.000000
284
FIG. 5
turbine booster surge

controller 284 exit.

80.00
65.00
0.000000
285
FIG. 5
turbine booster surge

controller check valve

outlet

80.00
65.00
0.000000
285
FIG. 5
turbine booster surge

check valve 285 inlet

−155.00
420.00
900000.000000
288
FIG. 4
temp out of 152 pre

heater on gas nitrogen to

turbine expanders FIG.

5, (510 FLOW = 528

FLOW)

−155.00
420.00
900,000.000000
288
FIG. 5&4
from FIG. 4 point 288, to

here

−155.00
420.00
180,000.000000
289
FIG. 5
inlet flow controller, sets

the guide veins

−155.00
420.00
180,000.000000
290
FIG. 5
inlet flow controller, sets

the guide veins

−155.00
420.00
180,000.000000
291
FIG. 5
inlet flow controller, sets

the guide veins

−155.00
420.00
360,000.000000
292
FIG. 5
inlet flow controller, sets

the guide vanes

−292.66
37.93
2000.000000
300
FIG. 1
liquid oxygen removed

from LPC 116 to SC 117

(psia)

−298.00
34.93
2000.000000
301
FIG. 1
liquid oxygen from SC

117 to auto control valve

(open or closed) (psia)

−298.00
23.93
2000.000000
302
FIG. 1&8
liquid oxygen to oxygen

filter system. FIG. 8

(psia)

−298.00
23.93
2,000.000000
302
FIG. 8&1
ASU liquid oxygen to

filter box, from FIG. 1

psia

−298.00
24.00
161521.037842
305
FIG. 4&8
Liquid oxygen to FIG. 8

−298.00
24.00
161,521.037842
305
FIG. 8&4
inlet liquid oxygen from

liquefier from FIG. 4

psia

−298.00
23.89
161521.037842
310
FIG. 8
inlet check valve liquid

oxygen to filter box FIG.

8, psia

−298.00
23.89
0.000000
311
FIG. 8
relief valve on the liquid

oxygen header psia

−298.00
23.89
0.000000
312
FIG. 8
auto control valve liquid

oxygen to dump system

psia

−298.00
23.89
161521.037842
313
FIG. 8
auto control valve liquid

oxygen to storage system

psia

−298.00
23.88
0.000000
314
FIG. 8
relief valve on the double

block and bleed psia

−298.00
23.88
0.000000
315
FIG. 8
auto control valve double

block and bleed vent psia

−298.00
23.88
161521.037842
316
FIG. 8
auto control valve liquid

oxygen to storage system

psia

−292.66
21.93
161521.037842
320
FIG. 1
gas oxygen removed

from LPC 116. To cold

side of MHE 113. (psia)

37.00
19.93
161521.037842
321
FIG. 1&3
gas oxygen removed

from MHE 113 warm

side to FIG. 3 point 321.

(psia)

37.00
19.93
161521.037842
321
FIG. 3&1
Low pressure oxygen

gas flow from 113 FIG. 1

37.00
19.92
161521.037842
325
FIG. 3
Inlet flow meter, control

feed flow set by ASU

37.00
19.90
161521.037842
326
FIG. 3
Oxygen inlet to liquefier

auto flow control valve

37.00
19.89
0.000000
327
FIG. 3
over load flow meter

37.00
14.70
0.000000
328
FIG. 3
relief valve EXIT

37.00
14.70
0.000000
329
FIG. 3
over load auto vent valve

EXIT

37.00
19.89
161521.037842
330
FIG. 3
inlet to liquefier check

valve

37.00
19.87
161521.037842
331
FIG. 3
Gas oxygen to liquefier

flow meter.

37.00
19.86
161521.037842
332
FIG. 3&4
Oxygen inlet to liquefier

FIG. 4

37.00
19.86
161521.037842
332
FIG. 4&3
Oxygen gas from FIG. 3

to here

−298.00
23.93
2000.000000
335
FIG. 8
liquid oxygen from asu

to oxygen filter check

valve psia

−298.00
23.93
0.000000
336
FIG. 8
entry to oxygen dump or

bypass filters psia

80.00
14.70
0.000000
337
FIG. 8
relief valve on the double

block and bleed psia

80.00
14.70
0.000000
338
FIG. 8
asu liquid oxygen to

dump system psia

80.00
14.70
0.000000
339
FIG. 8
liquid oxygen to bypass

the filters psia

80.00
14.70
0.000000
340
FIG. 8
bypass double block and

bleed relief valve psia

80.00
14.70
0.000000
341
FIG. 8
bypass double block and

bleed vent valve psia

80.00
14.70
0.000000
342
FIG. 8
bypass liquid oxygen

exit to storage psia

−298.00
23.93
2000.000000
343
FIG. 8
asu liquid oxygen entry

valve to filter 175, psia

−298.00
23.92
0.000000
344
FIG. 8
relief valve on the double

block and bleed psia

−298.00
23.92
0.000000
345
FIG. 8
double block and bleed

vent valve psia

−298.00
23.92
2000.000000
346
FIG. 8
inlet valve to filter 175,

psia

−298.00
0.00
0.000000
347
FIG. 8
delta pressure controller

for 175

−298.00
0.00
0.000000
348
FIG. 8
temperature indicator

and controller for 175

−298.00
22.92
0.000000
349
FIG. 8
relief valve on the double

block and bleed psia

−298.00
22.92
0.000000
350
FIG. 8
double block and bleed

vent valve psia

−298.00
22.92
0.000000
351
FIG. 8
inlet to cool down system

to 176 psia

−298.00
22.92
1999.101368
352
FIG. 8
inlet to double block and

bleed exit psia

−298.00
22.91
0.000000
353
FIG. 8
relief valve on the double

block and bleed psia

−298.00
22.91
0.000000
354
FIG. 8
double block and bleed

vent valve psia

−298.00
22.91
1999.101368
355
FIG. 8
filter 175 to storage

header psia

−298.00
23.93
0.000000
356
FIG. 8
inlet asu liquid oxygen

header relief valve psia

−298.00
23.93
0.000000
357
FIG. 8
asu liquid oxygen entry

valve to filter 176 psia

80.00
14.70
0.000000
358
FIG. 8
relief valve on the double

block and bleed psia

80.00
14.70
0.000000
359
FIG. 8
double block and bleed

vent valve psia

80.00
14.70
0.000000
360
FIG. 8
inlet valve to filter 176,

psia

80.00
0.00
0.000000
361
FIG. 8
delta pressure controller

for 176

−155.00
0.00
0.000000
362
FIG. 8
temperature indicator

and controller for 175

−155.00
63.00
0.000000
363
FIG. 8
relief valve on the double

block and bleed psig

−155.00
63.00
121.567188
364
FIG. 8
double block and bleed

vent valve psig

−155.00
63.00
0.000000
365
FIG. 8
inlet to cool down system

to 175, psig

−155.00
63.00
0.000000
366
FIG. 8
inlet to double block and

bleed exit psig

80.00
14.70
0.000000
367
FIG. 8
relief valve on the double

block and bleed psia

80.00
14.70
0.000000
368
FIG. 8
double block and bleed

vent valve psia

80.00
14.70
0.000000
369
FIG. 8
filter 176 to storage psia

80.00
14.70
0.000000
370
FIG. 8
cool down double block

and bleed relief valve

psia

80.00
14.70
0.000000
371
FIG. 8
cool down double block

and bleed vent valve psia

80.00
14.70
0.000000
372
FIG. 8
cool down auto flow

control valve psia

80.00
14.70
0.000000
373
FIG. 8
cool down check valve

psia

80.00
14.70
0.000000
374
FIG. 8
cool down system relief

valve psia

80.00
14.70
0.000000
375
FIG. 8
flow indicator and

controller of the cool down

system psia

80.00
14.70
0.000000
376
FIG. 8
double block and bleed

vent valve psia

80.00
14.70
0.000000
377
FIG. 8
cool down auto valve inlet

to 175, psia

80.00
14.70
0.000000
378
FIG. 8
cool down auto valve inlet

to 176, psia

−298.00
20.00
0.000000
379
FIG. 8
storage header relief

valve psia

−298.00
20.00
0.000000
380
FIG. 8
double block and bleed

vent and purge

valve, psia

−298.00
19.99
163520.139210
381
FIG. 8
liquid oxygen to storage

tank psia

−298.00
15.70
100.000000
382
FIG. 8
oxygen storage tank vent

psia

−304.00
18.11
7286.413203
400
FIG. 1&2
Gas out Crude argon

phase separator 112

(psia) to FIG. 2

−304.00
18.11
7286.413203
400
FIG. 2&1
crude argon to AHE 133

cold side.

98.00
15.00
7286.413203
401
FIG. 2
Crude argon out of the

AHE 133 warm side

102.00
50.50
7368.313118
402
FIG. 2
into the warm side of the

combusted argon heat

exchanger

80.00
16.34
205.000000
403
FIG. 2
Out of the 128 to control

valve hydrogen excess

return

98.00
15.00
7491.413203
404
FIG. 2
inlet to AP 134. crude

Argon hydrogen

240.00
60.00
7491.413203
405
FIG. 2
exit of AP 134 to after-

cooler 135

88.00
58.00
7491.413203
406
FIG. 2
exit after cooler 135

80.00
3500.00
240000.000000
407
FIG. 2
From Hydrogen tube

trailer 136 to control

valve

80.00
60.00
353.412813
408
FIG. 2
After control valve extra

hydrogen feed

88.00
56.00
7844.826016
409
FIG. 2
Blended crude argon and

hydrogen into argon

flash arrester 137

87.00
56.00
7844.826016
410
FIG. 2
into argon deoxo 138

900.00
55.00
7368.313118
411
FIG. 2
into combusted argon

after cooler 139

88.00
54.50
7368.313118
412
FIG. 2
into combusted argon

water separator 140

88.00
54.00
7368.313118
413
FIG. 2
into combusted argon

dryer bed on line 141

104.00
52.00
7368.313118
414
FIG. 2
into combusted argon

dust filter 143

−282.00
42.15
7368.313118
415
FIG. 2
Out of the cold side of

the combusted argon

heat exchanger 113 to

hydrogen separator 127

−297.00
40.11
7163.313118
416
FIG. 2
Gas from 127 to hydrogen

separator condenser

tube side 128

−297.00
40.11
7163.313118
417
FIG. 2
Liquid from 128 tube

side hydrogen separator

condenser return to 127

−297.00
40.11
7163.313118
418
FIG. 2
Argon and nitrogen liquid

from hydrogen separator 127

−298.00
40.00
205.000000
419
FIG. 2
hydrogen gas from tube

side of the 128 to a

control valve

−297.00
25.11
7163.313118
420
FIG. 2
418 liquid argon and

nitrogen to tray 30

after control valve

−307.00
24.90
7587.889152
421
FIG. 2
Mostly gas nitrogen and

hydrogen gas off the top

of the pure argon column

−307.00
24.70
7587.889152
422
FIG. 2
All of the hydrogen gas,

and nitrogen gas from

the tube side of the 131

the condenser to the 132

separator

−307.00
14.70
67.748921
423
FIG. 2
All of the hydrogen gas

and a little nitrogen gas

from the 132 separator,

vent to atm.

−307.00
24.70
7520.140231
424
FIG. 2
Liquid nitrogen from

132 phase separator back

to the 38 tray of the 130

column

−297.00
26.00
7095.564197
425
FIG. 2
129 overflow of pure liquid

argon, now bottom

liquid of the 130 column,

Pure liquid argon to auto

control valve to storage

−297.00
20.00
7734.164975
427
FIG. 2
total liquid argon after

auto control valves to

storage

−250.00
20.00
425.733852
428
FIG. 2
124 Storage tank, gas off

to auto control valve

−250.00
20.00
212.866926
429
FIG. 2
123 Transport trailer, gas

off to auto control valve

−250.00
19.50
638.600778
430
FIG. 2
123 gas off, and 124 gas

off, after the auto control

valves to the tube side of

the 125 argon recondenser

−297.00
27.60
638.600778
431
FIG. 2
125 tube side recondensed

liquid argon to auto

control valve to storage

87.00
55.05
0.000000
432
FIG. 2
combusted argon water

out of phase separator

80.00
65.00
6500.000000
433
FIG. 2
argon dryer bed

reactivation vent

−287.00
84.00
900000.000000
450
FIG. 4&5
From FIG. 5 point 450

turbines exhaust to the

151 with 3% liquid droplets

−287.00
84.00
900,000.000000
450
FIG. 5
turbine discharge header

−286.00
80.00
2000.000000
451
FIG. 4
over produced liquid

nitrogen in the 151, major

flash off.

−286.00
80.00
5000.000000
452
FIG. 4
liquid nitrogen from 151

to oxygen flash pot

147 = high flash

−286.00
80.00
5000.000000
453
FIG. 4
liquid nitrogen from 151

to nitrogen production

flash pot 148

−286.00
80.00
15000.000000
454
FIG. 4
liquid nitrogen from 151

to pump flash pot 149

50.00
67.00
873000.000000
455
FIG. 4
higher pressure nitrogen

gas out of 145 boiler to

144 oxygen cooler then

through valve 455

45.00
66.50
1000.000000
456
FIG. 4
branch off to pre heater

152

45.00
66.50
1066190.000000
457
FIG. 4
controlling valve to add

back pressure for 456 to

cross the pre heater 152

43.00
65.00
1067190.000000
458
FIG. 4&5
TEMP CHANGE, point

458 to FIG. 5

43.00
65.00
1,067,190.000000
458
FIG. 5
from point 458 FIG. 4 to

here

−316.30
18.00
5000.000000
459
FIG. 4
gas nitrogen out of the

148 nitrogen production

flash pot to 150 ADDED

COOLING HEAT

EXCHANGER

−300.00
18.00
15000.000000
460
FIG. 4
gas nitrogen out of shell

side of 149 pump flash

pot

−300.00
18.00
15000.000000
460
FIG. 4
low pressure cool nitrogen

to 146 condenser

from 149 shell side

−316.00
18.00
5000.000000
461
FIG. 4
gas nitrogen out of the

shell side of the 147 oxygen

production flash pot

−316.00
18.00
5000.000000
461
FIG. 4
low pressure cool nitrogen

to condenser from 461

45.00
66.50
1067190.000000
462
FIG. 4
ref point 462

90.00
111.82
1465374.701923
500
FIG. 4&5
from FIG. 5, major flow

into the liquefier from

the 168 after cooler

90.00
111.82
1,465,374.701923
500
FIG. 5&4
flow not taken by surge

controller 284, now to

500. FIG. 4

90.00
111.82
1465374.701923
501
FIG. 4
one of three branch off

of point 500, to the 144

oxygen cooler

90.00
111.82
426895.739765
502
FIG. 4
one of three branch off

of point 500, bypass

90.00
111.82
300000.000000
503
FIG. 4
one of three branch off

of point 500, to the 152

per heater

−299.00
100.00
900000.000000
510
FIG. 4&6
liquid nitrogen to the

recirculation pump FIG. 6,

PUMP HOUSE

−299.00
100.00
900000.000000
510
FIG. 6&4
from FIG. 4, this is the

pump inlet flow or by-

pass

−299.00
100.00
10892.152969
511
FIG. 4&6
liquid nitrogen to FIG. 6

feed to ASU

−299.00
100.00
10892.152969
511
FIG. 6&4
Liquid nitrogen from

FIG. 4 to dump or return

to asu

0.00
0.00
0.000000
512
FIG. 4
liquid nitrogen to shell

side of the 149 pump flash

pot off of production =

low flash

0.00
0.00
0.000000
513
FIG. 4
liquid nitrogen to the

shell side of the 147 oxygen

production flash pot

from production = low

flash

0.00
0.00
0.000000
514
FIG. 4
liquid nitrogen to the

shell side of the 148

nitrogen production flash

pot off of production =

low flash

−310.00
90.00
554482.548954
515
FIG. 4&6
production liquid nitrogen

to storage FIG. 6

−310.00
90.00
554482.548954
515
FIG. 6&4
from FIG. 4, liquid nitrogen

to storage or dump

−299.00
100.00
900000.000000
520
FIG. 6
valve inlet to pump 169

−299.00
100.00
0.000000
521
FIG. 6
valve inlet to pump 170

−299.00
100.00
0.000000
522
FIG. 6
pump bypass to 145

boiler FIG. 4

−299.00
100.00
0.000000
523
FIG. 6
pump bypass to boiler

check valve

−260.00
420.00
900000.000000
524
FIG. 6
outlet valve from pump

169

80.00
14.70
0.000000
525
FIG. 6
outlet valve from pump

170

−260.00
420.00
900000.000000
526
FIG. 6
Pump 169 exit check

valve

80.00
14.70
0.000000
527
FIG. 6
Pump 170 exit check

valve

−286.00
100.00
900000.000000
528
FIG. 4&6
pumped liquid nitrogen

from FIG. 6 to the 145

boiler

−260.00
420.00
900000.000000
528
FIG. 6&4
liquid nitrogen to FIG. 4,

for the 145 boiler

0.00
0.00
0.000000
529
FIG. 4&6
pumped liquid nitrogen

from FIG. 6 to the shell

side of the 149 pump

flash pot

−260.00
420.00
0.000000
529
FIG. 6&4
liquid nitrogen to pump

flash pot 149 FIG. 4

−286.00
90.00
0.000000
530
FIG. 4
Pumped liquid nitrogen

inlet of the shell side of

the 149 pump flash pot =

high flash off.

80.00
14.70
0.000000
535
FIG. 6
last purge point before

inlet to nitrogen storage

80.00
14.70
0.000000
536
FIG. 6
last purge valve

−310.00
90.00
554482.548954
537
FIG. 6
storage entry valve

−310.00
15.70
500.000000
538
FIG. 6
storage tank vent valve

80.00
14.70
0.000000
539
FIG. 6
NITROGEN TANK

PUMP BACK

80.00
14.70
0.000000
540
FIG. 6
PUMP BACK VALVE

80.00
14.70
0.000000
541
FIG. 6
PUMP BACK CHECK

VALVE

−299.00
14.70
0.000000
542
FIG. 6
LIQUIFER NITROGEN

TO DUMP

−299.00
100.00
10892.152969
543
FIG. 6
LIQUIFER NITROGEN

TO ASU

−299.00
100.00
10892.152969
544
FIG. 1&6
from FIG. 6, liquid

nitrogen from liquifer

return flow to asu

−299.00
100.00
10892.152969
544
FIG. 6&1
to FIG. 1 liquid nitrogen

return to ASU

−314.00
59.00
8547.152969
545
FIG. 1&2
CROSS OVER POINT

545 TO FIG. 4 (psia)

−314.00
59.00
8547.152969
545
FIG. 2&1
Liquid nitrogen from

FIG. 1 to 126 and 131.

−314.00
35.00
747.152969
546
FIG. 2
liquid nitrogen after

level control valve to

126

−310.00
22.00
7800.000000
547
FIG. 2
Liquid nitrogen after

level control valve to

131

−314.00
59.00
2345.000000
548
FIG. 1
FIG. #1 part of the

liquefier feed back to the

plant before the control

valve (psia)

−317.40
17.31
2345.000000
549
FIG. 1
liquid nitrogen from liquefier

after control valve (psia)

−308.00
35.00
747.152969
555
FIG. 2
gas nitrogen off of the

126 to a pressure control

valve

−310.00
22.00
7800.000000
556
FIG. 2
gas nitrogen off of the

131 to a pressure control

valve

−315.00
17.80
8547.152969
557
FIG. 2
gas from 126 and 131 after

the pressure control

valves

−315.00
17.80
8547.152969
558
FIG. 1
gas nitrogen from the

pure argon system, cross

over from FIG. 4 (psia)

−315.00
17.80
8547.152969
558
FIG. 2&1
gas nitrogen to FIG. 1

−280.00
80.00
873000.000000
450 −
ref
turbine exhaust gas from

(452 +

450 after 151 to 146

453 +

condenser

454 +

451)

−316.00
18.00
7000.000000
459 +
ref
low pressure cool nitrogen

451

to condenser from

459 + 451

ref
ref
20000.000000
460 +
ref
460 + 459 cold gas nitrogen

459

to added cooling

heat exchanger

90.00
65.52
398,184.701923
ref
ref
flow not taken by surge

controller 281, now to

283

−255.00
17.00
27000.000000
ref
ref
combined low pressure

nitrogen gas to boiler

90.00
41.32
398,184.701923
REF
REF
flow not taken by surge

controller 278, now to

280

−245.00
80.00
873000.000000
ref
ref
combined high pressure

nitrogen gas to boiler

ref
ref
900000.000000
ref
ref
cold nitrogen gas to the

condenser 146

The liquefier presented herein will boil liquid nitrogen to generate running gas pressures for the turbines. The liquefier is designed to work with an air separation plant, running at a stable state. The air separation plant will supply a steady stream of gaseous nitrogen and oxygen from the main heat exchanger warm end. Then, from the new liquefier, a stream of sub cooled liquid nitrogen and liquid oxygen will be sent to storage, along with a small amount of liquid nitrogen that will be returned to the air separation plant to make liquid oxygen in the low pressure column, and liquid argon both to storage. The air separation plant will be running at a reduced pressure due to the low pressure column's lower pressure. The air separation plant will be running on a maximum oxygen gas removal mode. The air separation plant, with a MAC flow like shown above, and this presented liquefier will produce liquid argon, and 2,000 scfh oxygen liquid needed to keep the hydrocarbons under 5% and remove all the krypton and xenon solids that would normally build up in the low pressure column's reboiler and be cleaned up in the oxygen filters. The plant can run a lower pressure by having almost all the oxygen removed as a gas, then oxygen gas will be liquefied in this invention, then put to storage as sell able product. The liquefaction of the oxygen gas from the low pressure column, that is not needed for a pipe line gas customer can then take place in the present liquefier. All the gas nitrogen that is not needed for a pipe line customer can be liquefied in the presented liquefier.

The presented liquefier will produce sell able liquid for less cost than what is being used today. The compressing of gas to a pressure needed to make liquid costs a lot of money. The temperature of the liquids to storage can be adjusted to meet the storage tank positive pressure requirements. The sub cooler in the distillation cold box has no control passed original design for reducing the liquid oxygen to storage temperature. This invention gives the control. The oxygen filter system can be used on any plant making liquid oxygen. This will produce liquid oxygen with less contamination. This liquefier can be placed at the end of a long pipe line to liquid at remote location. This will reduce shipping cost, and reduce truck traffic around the main plant. This liquefier can also be placed on-board a ship moving liquefied natural gas. This will keep the liquid cold to stop the venting.

While the present invention has been described at some length and with considerable particularity with respect to the several described embodiments and particularly with respect to the particular and principal intended embodiment, it is not intended that it should be limited to any such particulars or embodiments or any particular preferred embodiment but is to be construed with reference to the particular appended claims so as to provide the broadest possible interpretation of such claims in view of the prior art and, therefore, to effectively encompass the effective and intended scope of the invention with respect both to apparatus for practicing the invention and to methods of performing and practicing the invention. As used throughout, ranges are used as shorthand for describing each and every value that is within the range. Any value within the range can be selected as the terminus of the range.

Claims

1. A liquefier device configured for use with an air separation plant producing oxygen and nitrogen gas comprising: an inlet piping system to the liquefier device,an insulated box having a low pressure nitrogen gas purge feed to keep the insulated box dry, the box housing a plurality of multi-pass counter current flow heat exchangers each having a warm side and a cold side, a high pressure nitrogen bath boiler, a plurality of turbine expanders connected in parallel, a turbine exhaust phase separator, an oxygen production flash pot, a nitrogen production flash pot, and a nitrogen pump flash pot,the inlet piping system connecting to a piping and valve system of the liquefier device and including a take or vent gas oxygen inlet line into the insulated box, a take or vent low pressure column gas nitrogen inlet line, and a take or vent high pressure column gas nitrogen inlet line,said oxygen production, nitrogen production, and nitrogen pump flash pots and boiler each having a tube bank side and a shell side, the tube banks in said flash pots and boiler being partly submerged by a liquid nitrogen bath held by the shell side, the flash pots each having a liquid height controllable by multiple automatic liquid level control valves, and the boiler having a variable speed pump that will replenish the liquid in the boiler shell side,a plurality of turbine boosters connected in series, each of said turbine boosters having an operably associated fan cooled turbine booster aftercooler and surge valve,said multi-pass counter current flow heat exchangers including an oxygen cooler for cooling a flow of oxygen gas from the take or vent gas oxygen inlet line, a preheater for heating a flow of vaporized nitrogen produced by the boiler prior to entering the turbine expanders, an added cooling heat exchanger, and a condenser,each of the turbine expanders and turbine boosters having an operably associated inlet flow meter, and each of the turbine expanders having variable guide vanes and operably connected to one of the turbine boosters,the take or vent gas oxygen inlet line connected to pass the flow of oxygen gas sequentially through the oxygen cooler, boiler, and condenser, into the tube side of the oxygen production flash pot, and exiting the oxygen production flash pot as a subcooled liquid oxygen ready for storage,the take or vent low pressure column gas nitrogen inlet line joining a low pressure nitrogen gas line downstream from an auto pressure control valve on the oxygen cooler warm side, supplying a joined low pressure flow to a first of the plurality of turbine boosters, the low pressure nitrogen gas line containing vaporized liquid nitrogen from the shell side of the pump flash pot, the shell side of the nitrogen production flash pot, the shell side of the oxygen production flash pot, and from an exit of an auto liquid level control valve in a line off of the turbine exhaust phase separator,the joined low pressure flow being compressed in the first turbine booster and reduced in temperature in the aftercooler associated with the first turbine booster, and then being further compressed and reduced in temperature in at least one additional turbine booster and associated aftercooler before joining a line containing a combined flow of nitrogen gas from the take or vent high pressure column gas nitrogen inlet line and a high pressure gas line after exiting the oxygen cooler warm side, supplying a major nitrogen gas flow to a last of said turbine boosters and associated aftercooler,the major nitrogen gas flow upon exiting the aftercooler associated with the last turbine booster in a major flow line holding a heat of compression, said major flow line branching into a branch line to the oxygen cooler warm side, a branch line to the preheater warm side, and a bypass line, the branch and bypass lines recombining into the major flow line downstream from the oxygen cooler and preheater and sequentially entering one of the tube banks in the boiler and then the condenser, the major nitrogen gas flow providing a warm flow to the boiler which boils the liquid nitrogen bath in the boiler, and undergoing a heat exchange in the condenser with a gas flow in the high pressure gas line from the turbine expander phase separator, transforming the major nitrogen gas flow to a two-phase liquid gas nitrogen stream which is passed into the added cooling heat exchanger warm side, and then into the nitrogen pump flash pot tube bank to produce a single phase liquid nitrogen stream,a plurality of branch lines off of the nitrogen pump flash pot tube bank in which the single phase liquid nitrogen stream is directed, including a branch line to a nitrogen pump system which brings the single phase liquid nitrogen stream up in pressure, and a first line exiting the nitrogen pump system feeding the increased pressure stream to the boiler shell side to boil the increased pressure stream to a vapor point, anda line containing the flow of vaporized nitrogen produced by the boiler sequentially feeding the preheater and the turbine expanders connected in parallel, an exhaust flow carried in an exhaust line connected to an exit of the turbine expanders to the turbine exhaust phase separator, a nitrogen gas flow exiting the turbine exhaust phase separator in a line connecting to the high pressure gas line before entering the condenser cold side, and a liquid nitrogen flow exiting the turbine exhaust phase separator in lines connecting to the flash pots and to the line connecting to the low pressure nitrogen gas line.
2. The liquefier device of claim 1 wherein each of the aftercoolers is a dual air cooling fan system set to hold a controllable temperature on the joined low pressure flow and major nitrogen gas flow upon exit from the aftercoolers, and in which one fan is a variable pitch fan.
3. The liquefier device of claim 1 in which the nitrogen pump system additionally comprises a secondary nitrogen pump to enable continuous operation during maintenance, and a pump bypass line off of the branch line connecting to the first line.
4. The liquefier device of claim 1 in which the boiler tube banks are moving the flow of oxygen gas, the increased pressure single phase liquid nitrogen stream supplied to the boiler shell side by the nitrogen pump system, the nitrogen gas flow from the turbine exhaust phase separator, and the major nitrogen gas flow, wherein the increased pressure single phase liquid nitrogen stream supplied to the boiler shell side by the nitrogen pump system is at a higher pressure than the other gases in the boiler tube banks, causing a boiling action such that the increased pressure single phase liquid nitrogen stream will exit the boiler as the flow of vaporized nitrogen to the preheater.
5. The liquefier device of claim 1 in which one pass in the preheater is the branch line off of the major flow line to the preheater warm side, another pass is a branch line off of a line containing the joined low pressure flow after the first turbine booster aftercooler exhaust, another pass is a branch line off of the take or vent high pressure column gas nitrogen inlet line, and another pass is the line containing the flow of vaporized nitrogen from the boiler shell side prior to entering the turbine expanders, and wherein a temperature control valve in the branch line off of the line containing the joined low pressure flow line after the first turbine booster aftercooler exhaust controls an inlet temperature of the flow of nitrogen gas to the turbine expanders.
6. The liquefier device of claim 1 in which the major nitrogen gas flow directed into the branch line off of the major gas line to the oxygen cooler provides a source of heat which heat maintains an exit temperature of the vaporized liquid nitrogen in the low pressure nitrogen gas line and the nitrogen gas flow in the high pressure gas line within a predetermined range of an inlet temperature of the oxygen gas flow in the take or vent oxygen inlet line into the oxygen cooler on the warm side by using an auto control valve to further open or restrict the major nitrogen gas flow in the branch line off of the major gas line to adjust the exit temperatures when outside of the predetermined range.
7. The liquefier device of claim 1 in which the condenser brings the major nitrogen gas flow to a two-phase liquid gas stream and cools the flow of oxygen gas.
8. The liquefier device of claim 1 in which the liquid nitrogen flow from the turbine from the turbine exhaust phase separator is directed to three auto liquid level control valves each connecting to the shell side of one of the flash pots for replenishing the liquid level of the flash pots, and to the auto liquid level control valve in the line off of the turbine exhaust phase separator to the low pressure gas line, wherein liquid nitrogen not used by the flash pots is directed into the low pressure gas line prior to the low pressure gas line entering the condenser on the cold side.
9. The liquefier device of claim 8 in which the nitrogen gas flow from the turbine exhaust phase separator in the high pressure gas line and the vaporized liquid nitrogen in the low pressure gas line are a refrigeration source of the condenser.
10. The liquefier device of claim 8 in which the exhaust flow in the exhaust line from the turbine expanders to the turbine exhaust phase separator contains about three percent liquid nitrogen droplets.
11. The liquefier device of claim 8 in which the added cooling heat exchanger is a three-pass counter current flow heat exchanger, wherein a first nitrogen gas flow in the low pressure gas line off of the nitrogen production flash pot low pressure shell side gas enters the cold side and exits the warm side of the added cooling heat exchanger, a second nitrogen gas flow from the nitrogen pump flash pot low pressure shell side gas enters the cold side and exits the warm side of the added cooling heat exchanger, and the major nitrogen gas flow from the cold side exit of the condenser enters the warm side and exits the cold side of the added cooling heat exchanger, said first and second nitrogen gas flows cooling the major nitrogen gas flow to the nitrogen pump flash pot tube bank side.
12. The liquefier device of claim 1 in which the single phase liquid nitrogen stream from the nitrogen pump flash pot to the nitrogen pump system is temperature monitored by controlling the liquid nitrogen height of the shell side of the nitrogen pump flash pot and the pressure of the nitrogen bath is held back by an auto pressure control valve so that the temperature of the increased pressure single phase liquid nitrogen stream in the first line exiting the nitrogen pump system and feeding the boiler is not too cool to stop the boiling action or so a majority of the increased pressure single phase nitrogen stream in the first line does not flash upon entry into the shell side of the boiler.
13. The liquefier device of claim 1 in which the oxygen cooler is a four pass counter-current flow heat exchanger, of which the oxygen gas flow from the take or vent inlet piping line enters the warm side and exits the cold side, the vaporized liquid nitrogen in the low pressure gas line enters the cold side and exits the warm side, the nitrogen gas flow in the high pressure gas line enters the cold side and exits the warm side, and the major nitrogen gas flow in the branch line from the major gas line enters the warm side and exits the cold side, said major nitrogen gas flow set to warm the oxygen cooler.
14. The liquefier device of claim 1 in which the preheater is a four pass counter-current flow heat exchanger, of which (1) the branch line off of the major nitrogen gas line contains a controlled partial flow off of the major nitrogen gas flow which enters the preheater warm side and exits the cold side, (2) the line containing the flow of vaporized nitrogen from the shell side of the boiler enters the preheater cold side and exits the warm side, (3) another line is a branch line off of the joined low pressure flow line exiting from the first turbine booster aftercooler which enters the preheater warm side and exits the cold side, and (4) another line contains a flow of gas nitrogen which is a branch flow off of a combined flow line from the take or vent high pressure column nitrogen gas inlet line and the high pressure gas line which enters the warm side and exits the cold side, wherein the branch line off of the major nitrogen gas line, the branch line off of the joined low pressure line, and the line containing a branch flow off of the combined flow line are connected to control valves for controlling said flows which add heat to the heat exchanger.
15. The liquefier device of claim 1 in which the condenser is a six pass counter-current flow heat exchanger, including (1) the flow of oxygen gas from the take or vent gas oxygen inlet line which enters the warm side and exits the cold side of the condenser and which serves as a heat source to the condenser, (2) a flow of gas nitrogen in a line exiting the oxygen flash pot shell side which is a boiled off nitrogen gas which enters the cold side and exits the warm side of the condenser and acts as a refrigerant, (3) a flow of gas nitrogen in the low pressure gas line exiting the nitrogen production flash pot shell side which is a boiled off nitrogen gas passing through the added cooling heat exchanger exiting the warm side combined with the vaporized liquid nitrogen exiting the auto liquid level control valve in the line connected to the turbine exhaust phase separator that will flash upon exiting said valve, which flow enters the cold side and exits the warm side, (4) the nitrogen gas flow exiting a gas side of the turbine exhaust phase separator which enters the cold side and exits the warm side of the condenser, (5) a flow of gas nitrogen exiting the nitrogen pump flash pot shell side which enters the cold side and exits the warm side of the condenser after passing through the added cooling heat exchanger, and (6) the major nitrogen gas flow in the major nitrogen line which enters the warm side and exits the cold side of the condenser, and is a heat source to the condenser, said major nitrogen gas flow undergoing a phase change from gas to a two phase liquid gas in the condenser.
16. The liquefier device of claim 1 in which a first tube bank in the boiler contains the oxygen gas flow, a second tube bank in the boiler contains the vaporized liquid nitrogen off of the shell side of the flash pots and the exit of the auto liquid level control valve in the line connected to of the turbine exhaust phase separator, a third tube bank in the boiler contains the gas nitrogen flow from the turbine exhaust phase separator which enters the cold side and exits the warm side of the boiler, and a fourth tube bank in the boiler contains the major nitrogen gas flow, and the increased pressure single phase liquid nitrogen stream in the first line from the liquid nitrogen pump system to the boiler shell side, which exits the boiler in the flow line exiting the boiler shell side as the flow of vaporized nitrogen which is sent to the cold side of the preheater.
17. The liquefier device of claim 1 in which the flow of oxygen gas into the oxygen production flash pot tube bank submerged in a liquid nitrogen bath held by the shell side is changed from a gas phase oxygen to a subcooled liquid oxygen, wherein the liquid height of the shell side liquid nitrogen bath is monitored to control the height of the subcooled liquid oxygen in the tube bank.
18. The liquefier device of claim 1 in which the single phase liquid nitrogen stream exits the nitrogen pump flash pot tube bank as a subcooled liquid nitrogen to five branch off lines, including the branch line to the nitrogen pump system, a line connecting to the shell side of the nitrogen pump flash pot, a line connecting to the oxygen production flash pot, a line connecting to a nitrogen liquid return to the air separation plant, and a line connecting to the nitrogen production flash pot tube bank which will then exit to two branch off lines at another subcooled temperature, to the nitrogen storage tank, and to a valve to hold a liquid level controlled height of the nitrogen production flash pot.
19. The liquefier device of claim 1 in which the nitrogen production flash pot liquid level of the shell side is replenished by either nitrogen liquid from the turbine exhaust phase separator and/or from the nitrogen production flash pot tube side back to the shell side of the nitrogen production flash pot.
20. The liquefier device of claim 1 in which a branch line off of the joined low pressure flow after the first turbine booster in the series of turbine boosters passes through the preheater to add heat to the preheater, and then connects back to the joined low pressure flow at a location downstream from the branch line.
21. The liquefier device of claim 1 in which a portion of the single phase liquid nitrogen stream from the nitrogen pump flash pot is connected in a branch line so as to be directed to an air separation plant supplying gas oxygen and nitrogen to the liquefier device.
22. The liquefier device of claim 21 in which a portion of the single phase liquid nitrogen stream from the nitrogen pump flash pot is connected to be sent back to the shell side of the nitrogen pump flash pot, to the shell side of the oxygen production flash pot, and to the tube side of the nitrogen production flash pot.
23. The liquefier device of claim 1 in which each turbine expander has a turbine with variable guide vanes and is operably connected to a turbine booster, said guide vanes holding back the nitrogen gas flow passing through the turbine expanders.
24. The liquefier device of claim 1 in which production liquid nitrogen from the nitrogen production flash pot is directed to a liquid nitrogen storage system.
25. The liquefier device of claim 4 in which the nitrogen gas flow from the turbine exhaust phase separator removes the latent heat of vaporization from the major nitrogen gas flow in the condenser.
26. The liquefier device of claim 1 additionally comprising a second line exiting the nitrogen pump system connecting back to the shell side of the nitrogen pump flash pot to the liquid nitrogen bath.

CROSS REFERENCE TO RELATED APPLICATIONS

This application claims the benefit of U.S. Provisional Application No. 62/506,932, filed May 16, 2016, which is incorporated herein by reference in its entirety.

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	Number	Date	Country
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Provisional Applications (1)

	Number	Date	Country
	62506932	May 2017	US

Apparatus and process for liquefying gases

Information

Patent Number

Date Filed

Date Issued

Inventors

Examiners

Agents

CPC

Field of Search

CPC

International Classifications

Abstract