Air separation

Abstract: In air separation method for supplying gaseous oxygen to meet the requirements of a variable demand cycle, air is rectified in a double rectification column 20 comprising high pressure column 22 and low pressure column 24. A liquid oxygen stream 46 is withdrawn from the column 24 and a nitrogen stream 34 from the column 72. The nitrogen stream 34 is warmed within a main heat exchanger 18. A variable part of it is expanded in turbine 76 to create plant refrigeration. When a demand for gaseous oxygen exists, a product stream formed of withdrawn liquid oxygen is raised by pump 62 to delivery pressure and at least part of the nitrogen stream is warmed to ambient temperature in heat exchanger 18, is compressed in compressor 70 and is then condensed against a vaporising product oxygen stream to form the gaseous oxygen. The resulting condensed nitrogen is then flashed into a tank 54. The flash vapour is added to the nitrogen stream upstream of its compression, thereby increasing the rate at which oxygen can be vaporised. Resultant liquid nitrogen condensate is introduced into the low pressure column 24 as reflux to allow the withdrawal of the liquid oxygen. Any excess amounts of the liquid oxygen and condensed nitrogen not immediately used are stored.

Description: The present invention relates to an air separation method for supplying gaseous oxygen in accordance with the requirements of a variable demand pattern. A variety of industrial processes have time varying oxygen requirements. For example, steel mini-mills utilise oxygen in the reprocessing of scrap steel. Since the scrap steel is processed by such mills in batches or heats, the demand for oxygen varies between a high demand phase during batch processing and a low demand phase between batch processing. In order to meet such oxygen demand requirements, air separation plants have been designed to supply gaseous oxygen in accordance with a variable demand pattern having high and low demand phases. Generally, such air separation plants store liquid oxygen during the low demand phase and liquid nitrogen during the high demand phase. Moreover, the liquid nitrogen and the gaseous oxygen product are produced by vaporising the stored liquid oxygen against condensing gaseous nitrogen produced by the plant. In one type of plant design, the gaseous oxygen product is directly supplied from the low pressure column of an air separation unit having a high pressure column operatively associated with the low pressure column by a condenser/reboiler. In such a plant design, the gaseous oxygen product is produced by evaporation of liquid oxygen in the low pressure column against condensation of gaseous nitrogen in the high pressure column. In another type of plant design condensation of nitrogen and evaporation of oxygen occur in heat exchangers external to an air separation plant rather than in low and high pressure columns of such a plant. An example of the type of air separation plant in which the gaseous product oxygen is supplied from the low pressure column is described in "Linde Reports on Science and Technology", No. 37, 1984. The plant disclosed in this publication supplies gaseous oxygen at a nominal production rate by extracting vaporised oxygen from the low pressure column. The oxygen vaporises against the condensation of nitrogen produced at the top of the high pressure column. A stream of the high pressure nitrogen is extracted from the high pressure column and is subsequently heated, compressed, cooled, and turboexpanded to supply plant refrigeration. In the plant described above, the amount of high pressure nitrogen extracted to supply plant refrigeration is controlled to adjust the amount of gaseous oxygen supplied, either above or below the nominal rate. During the high demand phase, the amount of high pressure nitrogen extracted from the high pressure column is reduced below that which is required to be extracted to produce gaseous oxygen at the nominal production rate. As a result, there is an increase in the degree to which liquid oxygen in the bottom of the low pressure column evaporates and high pressure nitrogen at the top of the high pressure column condenses. This produces an increase in the amount of liquid nitrogen collected at the top of the high pressure column which is extracted and stored in a storage tank. Liquid oxygen, stored in another storage tank during the low demand phase, is supplied to the low pressure column to replenish oxygen in the bottom of the low pressure column. During the low demand phase, the amount of high pressure nitrogen extracted from the high pressure column is increased over that required to be extracted in the production of oxygen at the nominal rate. This increases the amount of liquid oxygen collected at the bottom of the low pressure column because there is less high pressure nitrogen at the top of the high pressure column to condense. The increased amount of liquid oxygen collected in the low pressure column is extracted and stored for use in the high demand phase while previously stored high pressure nitrogen is introduced to the top of the low pressure column as reflux to wash down the oxygen and to add refrigeration. Processes of this design are limited by a ratio of maximum oxygen production to average oxygen production of about 1.5, owing to the means effected for varying the oxygen production rate. An example of an air separation plant in which evaporation and condensation of oxygen and nitrogen takes place in added heat exchangers and vaporisers is described in US Patent No 3,273,349. The air separation plant described in this patent is designed to supply liquid oxygen and waste nitrogen at nominal rates of production. During periods of low or no oxygen demand, liquid oxygen is stored in a storage vessel while liquid nitrogen, previously produced and stored during the high demand period is returned to the air separation plant for use as reflux to the low pressure column thereof. During periods of high demand, liquid oxygen from the storage vessel is pumped through a heat exchanger while waste nitrogen is compressed and is countercurrently passed through the heat exchanger. As a result, the liquid oxygen is vaporised for supply as product and the compressed nitrogen condenses and is stored for use during the low demand period. Design and operational problems exist in variable demand oxygen plants in which gaseous oxygen is supplied directly from the low pressure column. For instance, optimisation of the hydraulic design of the column and oxygen recovery over the full extent of the demand pattern are highly problematical. A major operational problem is that it is difficult to control the purity of the oxygen being recovered. Also, the oxygen that is recovered is supplied at too low a pressure to be utilised (without compression) in many industrial processes. As a consequence, the pressure of the oxygen must be increased by use of an oxygen compressor. It is to be noted that in variable demand oxygen plants in which oxygen is supplied by pumping liquid oxygen through a heat exchanger or vaporiser, the oxygen is supplied at a usable working pressure without the use of an oxygen compressor. However, while equipment costs may at least in part be saved in such a plant design, operating costs are increased in that there are energy losses involved in vaporising oxygen and condensing nitrogen outside the 'cold box' in which the rectification columns are housed. As may be appreciated, both types of plant designs involve the use of additional compressors and heat exchangers that in any event significantly add to plant cost and complexity. EP-A-0 102 190 discloses a process comprising steps (a) to (e) of claim 1 set out hereinbelow save that the oxygen product is continuously withdrawn from the lower pressure rectification column in gaseous state. The gaseous oxygen product is formed by continuous reboiling of liquid oxygen in the sump of the lower pressure rectification, the reboiling being effected by the condensing nitrogen in a condenser-reboiler thermally linking the higher pressure rectification column to the lower pressure rectification column. During periods of minimum demand for the oxygen product liquid oxygen is sent to storage from the lower pressure column and a shortfall in liquid nitrogen reflux for the lower pressure column is met from liquid nitrogen storage. During periods of maximum demand liquid nitrogen is returned from storage to the lower pressure rectification column, work-expansion of nitrogen is stopped so as to enable more nitrogen to be employed in the vaporisation of liquid oxygen and hence more gaseous oxygen to be produced, and excess nitrogen condensate is sent to storage. As will be discussed the present invention provides a method that is capable of supplying gaseous oxygen over a variable demand pattern at usable working pressures and over a wider range of demand than that contemplated in the known processes described above. While being totally integrated, the method of the present invention is far less complex than that involved in variable demand oxygen plants of the prior art. Additionally, column operation in a process of the present invention is very stable. This eliminates the design and operational problems associated with variable oxygen demand plants in which the oxygen is supplied directly from the low pressure column. According to the present invention there is provided a process for supplying gaseous oxygen to meet the requirements of a variable demand pattern including the steps of: a) continuously separating air into oxygen and nitrogen in a double rectification column comprising a higher pressure rectification column operatively associated with a lower pressure rectification column; b) continuously withdrawing nitrogen and liquid oxygen streams from the lower pressure rectification column; c) continuously condensing nitrogen separated in the higher pressure column and using one part of the resulting condensate as reflux in the higher pressure rectification column and another part thereof as reflux in the lower pressure rectification column; and d) continuously withdrawing a stream of nitrogen vapour from the higher pressure rectification column; e) expanding with the performance of external work at least a part of the stream of nitrogen vapour taken from the higher pressure rectification column so as to meet refrigeration requirements of the process; and f) when a demand for the gaseous oxygen exists, (i) pumping a product stream taken from the withdrawn liquid oxygen to a delivery pressure, diverting a stream of at least some of the said withdrawn nitrogen vapour from upstream of the said work expansion, warming by heat exchange said diverted nitrogen vapour stream, compressing the thus warmed nitrogen vapour stream, and heat exchanging the compressed nitrogen stream with the pumped product stream so as to vaporise the product stream and condense the compressed nitrogen stream; (ii) flashing a stream of the condensate formed by step (f) (i) to produce a two phase flow of nitrogen containing liquid and vapour phases and separating the liquid and vapour phases from one another; (iii) employing a stream of said liquid phase to supplement the reflux in the lower pressure rectification column; and (iv) adding a stream of the said vapour phase to the diverted nitrogen vapour to increase production of the gaseous oxygen; wherein at least some excess liquid oxygen is stored during periods of relatively low oxygen demand, and said stored liquid oxygen is used to increase oxygen production during periods of relatively high oxygen demand, and the rates at which nitrogen is expanded in step (e) and nitrogen is condensed in step (f) are varied with changing oxygen demand. Preferably, the addition of the said liquid phase to the lower pressure column as reflux is at a rate varying with the production of plant refrigeration such that the liquid oxygen is produced at an essentially constant rate. As may be appreciated, as the demand for gaseous oxygen decreases, the work expansion of nitrogen rich vapour increases so as to increase production of plant refrigeration. Operation of the process of the present invention to produce liquid oxygen at a constant rate facilitates column design. In addition, since liquid oxygen production is constant, it is simpler to maintain product purity than in known processes. It is to be noted from the above description that the main heat exchanger of the plant can be used to effect heat transfer between liquid oxygen and nitrogen to produce the gaseous oxygen product and the liquid nitrogen to be used as reflux. Moreover, a single nitrogen rich gas stream is thus used to serve three purposes, namely, to vaporise liquid oxygen, as reflux, and as a plant refrigerant. Such use of the nitrogen rich gas stream in itself allows a plant to be constructed that is simpler in layout and cost than known plant designs because additional compressors and expanders are not required. In addition, since the oxygen is supplied from outside the low pressure column, its pressure can be economically raised by pumping the liquid oxygen through the main heat exchanger rather than compressing the gaseous oxygen product with an oxygen compressor. The method according to the present invention will now be described by way of example with reference to the accompanying drawing; which is a flow diagram of air separation plant. In the ensuing description all values of pressure are given in absolute units. In addition, reference numerals designating streams also designate piping between the components to conduct the streams. The plant shown in the drawing is specifically designed to produce gaseous oxygen as a product having a purity of about 95.0 %. The oxygen produced by the air separation plant is supplied in accordance with a variable demand pattern having a high demand phase lasting about 32.0 minutes in which 279.77 moles/hr. of the oxygen at a temperature of about 18.9°C and a pressure of about 11.74 kg/cm² is supplied as a product. The rate of supply is roughly 1.87 times the plant's nominal production rate of oxygen. The demand cycle also has an alternating low demand phase following the high demand phase of approximately 28.0 minutes in which no gaseous oxygen is supplied. In operation, an air stream 10 at ambient temperature and pressure, (approximately 22.2°C and about 1.02 kg/cm²) and flowing at a flow rate of about 689.30 moles/hr is compressed in a compressor 12 to about 5.88 kg/cm². Preferably, air stream 10 is passed through an aftercooler 14, through which the air is cooled back to about 22.2°C. Air stream 10 then passes through a purifier 16 to remove carbon dioxide and water vapour from stream 10. Purifier 16 is composed of molecular sieve or a dual (unmixed) media of alumina and molecular sieve or alumina alone. After passage through purifier 16, air stream 10 undergoes a pressure drop of about 0.246 kg/cm², is subsequently further cooled in a main heat exchanger 18 to a temperature suitable for its rectification. Thereafter, air stream 10 is introduced into an air separation unit 20 having connected high and low pressure columns 22 and 24. Column 22 has about 21 trays and column 24 has about 39 trays. High and low pressure columns 22 and 24 are operatively associated with one another by a condenser/reboiler 26. Main heat exchanger 18 has a branched first pass 18a having a main segment 18b and a branch segment 18c. For purposes that will be discussed hereinafter, nitrogen rich vapour from high pressure column 22 fully warms in main segment 18b and partially warms in branch segment 18c. A second pass 18d is provided within main heat exchanger 18 to condense fully heated and compressed nitrogen rich vapour after having passed through main segment 18b of first pass 18a. This is accomplished by vaporising liquid oxygen passing through a third pass 18e of main heat exchanger 18. Forth and fifth passes 18f and 18g of main heat exchanger 18 are connected to high and low pressure columns 22 and 24, respectively, for cooling the air to the temperature suitable for its rectification against fully heating low pressure nitrogen from low pressure column 24. In high pressure column 22, the more volatile nitrogen rises and the less volatile oxygen falls from tray to tray and collects in the bottom of high pressure column 22 to form an oxygen-rich liquid 28 having a temperature of about -173.95°C and a pressure of about 5.52 kg/cm². A stream 30 of oxygen-rich liquid 28 is extracted from the high pressure column, is throttled through a valve 32, and is subsequently introduced into low pressure column 24 at about 29 trays from the top thereof for further separation. The more volatile nitrogen within high pressure column 22 collects at the top thereof as the aforementioned nitrogen rich gas, which for purposes that will be discussed hereinafter, is extracted from high pressure column 22 as a stream 34 having a substantially constant flow rate throughout the demand pattern of approximately 303.91 moles/hr. and a temperature of about -177.97°C. Such nitrogen-rich gas is also extracted as a stream 36 which is passed into condenser/reboiler 26, where it is condensed against liquid oxygen collecting in the bottom of low pressure column 24. A partial stream 38 of the condensed nitrogen is returned to the top of high pressure column 22 as reflux and another partial stream 40 of the condensed nitrogen is passed through a sub-cooler 42. After further cooling of partial stream 40 in sub-cooler 42, partial stream 40 is throttled through a flow control valve 44 and is introduced into the top of low pressure column 24 as reflux. Flow control valve 44 also acts to control the flow of reflux into both the low and high pressure columns to maintain nitrogen purity in the high pressure column. Liquid oxygen collected in the bottom of low pressure column 24, which has not been vaporised, is extracted from the bottom of low pressure column 24 as a stream 46 for reception within oxygen vessel 48. Oxygen vessel 48 is connected, at the top thereof, to low pressure column 24 via a line 50 so that the vapour pressure within oxygen vessel 48 is approximately equal to low pressure column 24. A stream 52 of low pressure nitrogen (mentioned above with respect to main heat exchanger 18) is withdrawn from the top of tow pressure column 24. Stream 52 has a temperature of approximately -193.20°C and a pressure of about 1.375 kg/cm². Stream 52 passes through sub-cooler 42 where it warms against the cooling of streams 40 and 56. Thereafter, stream 52 enters fifth pass 18g of main heat exchanger 18 to cool incoming air stream 10 flowing through forth pass 18f of main heat exchanger 18. Stream 52 is then discharged from the plant as waste nitrogen. Reflux is also supplied to low pressure column 24 from a flash tank 54 having a capacity of approximately 6000.0 litres. This reflux is necessary to allow the extraction of liquid oxygen from low pressure column 24. Excess amounts of liquid nitrogen, accumulated in flash tank 54 during the high demand phase, are extracted as a stream 56 which is further cooled in sub-cooler 42 against the warming of low pressure nitrogen stream 52. After such further cooling, stream 56 passes through a flow control valve 58 and is introduced into the top of low pressure column 24. As will be discussed in greater detail below, flow control valve 58 is used in metering the amount of reflux being supplied to low pressure column 24 such that liquid oxygen is produced in low pressure column 24 at an essentially constant rate. The following is a discussion of plant operation during the high demand phase. During the high demand phase, that is when a demand for gaseous oxygen exists, a product stream 60 composed of liquid oxygen from oxygen vessel 48 is pumped by a pump 62 through third pass 18e of main heat exchanger 18. The flow rate of product stream 60 is sufficient to meet the demand. In the illustrated embodiment and example, liquid oxygen stream 46 flows at about 148.17 moles/hr. into oxygen vessel 48. Product stream 60 of liquid oxygen is pumped from liquid oxygen collection vessel 48 by a pump 62 at a rate of approximately 279.77 moles/hr. and a delivery pressure of approximately 11.90 kg/cm² through third pass 18e of main heat exchanger 18. At the same time, flash vapour stream 64 is introduced into stream 34 which then flows along a flow path which includes main segment 18b of first pass 18a of main heat exchanger 18, a booster compressor 70, preferably an aftercooler 72, and then second pass 18d of main heat exchanger 18. Stream 34 fully warms in main heat exchanger 18 to a temperature of approximately 18.9°C. Stream 34, at about 5.32 kg/cm² is then compressed in booster compressor 70 to a pressure of about 30.45 kg/cm², is cooled by after cooler 72, and is condensed within second pass 18d of main heat exchanger 18 against vaporising product stream 60 concurrently passing through third pass 18e of main heat exchanger 18. After passage through main heat exchanger 18, product stream 60 heats to a temperature of approximately 18.9°C and undergoes a slight drop in pressure to about 11.70 kg/cm². Oxygen at such pressure can be supplied directly to a steel furnace without having to be compressed. Liquid nitrogen condensed from stream 34, designated in the drawings as stream 34a, is then flashed into flash tank 54 for production of stream 56 that, as has been discussed, is used as reflux in low pressure column 24. After condensation, stream 34a has a temperature of approximately -158.6°C and a pressure of approximately 30.10 kg/cm². Stream 34a is throttled through a valve 68 to a sufficiently low pressure to produce two phases within condensed stream 34. Valve 68 also serves to control condensation by the back pressure it creates. The liquid and vapour phases of the two phases separate in flash tank 54 to produce a liquid phase containing the liquid nitrogen to be introduced into low pressure column 24 as reflux and a vapour phase containing flash vapour used in forming flash vapour stream 64. Flash vapour stream 64 leaves flash tank 54 at a temperature of approximately -177.7°C and a pressure of about 5.62 kg/cm² and is throttled through a throttle valve 74 to equal the pressure of nitrogen-rich gas stream 34 which is effectively the pressure of high pressure column 22. It is to be noted that throttle valve 74 acts to control the amount of flash and to pressurise flash tank 54 so that stream 56 flows to low pressure column 24 without the use of a pump. During the high demand phase, stream 30 has a flow rate of approximately 375.62 moles/hr. and low pressure nitrogen stream 52 has a flow rate of approximately 396.95 moles/hr. The two reflux nitrogen streams, stream 40 and stream 56 respectively have flow rates of approximately 9.77 moles/hr. and 159.73 moles/hr. Both of such reflux nitrogen streams after passing through sub-cooler 42 are cooled to approximately -191.3°C, while stream 52 is warmed to a temperature of -182.2°C. Stream 52, after passage through main heat exchanger 18, is further warmed to about 18.9°C. During the low demand phase, stream 34 flows along an alternative flow path which consists of branch segment 18c of first pass 18a of main heat exchanger 18 to be partially heated and then expanded with the performance of the work in turboexpander 76. The resultant expanded stream 78 is then added back into the process to supply plant refrigeration. In main heat exchanger 18, stream 34 is partially heated to a temperature of about -158.3°C, and is then subsequently expanded from about 5.41 kg/cm² in turboexpander 76 to about 1.33 kg/cm² and about -191.3°C. The resultant turboexpanded stream 78 is combined with low pressure nitrogen stream 52 flowing at about 442.10 moles/hr. The combined stream is then sent through fifth pass 18g of main heat exchanger 18 at a flow rate of approximately 700.65 moles/hr. After leaving main heat exchanger 18, the combined stream heats to approximately 17.5°C. The addition of refrigeration acts to lower the enthalpy of air stream 10 before its entry into high pressure column 22. In this regard, air stream 10 in the low demand phase has a temperature of about -173.9°C arid a content of about 7.02% liquid. During the high demand phase, air stream 10 also has a temperature of about -173.9°C. Additionally, liquid oxygen at a rate of 150.84 moles/hr, essentially the same flow rate as in the high demand phase, is being removed as stream 46 from low pressure column 24. In order to maintain heat balance while keeping the liquid oxygen production rate essentially constant, valve 58 is set to reduce the flow rate of stream 56 to about 162.18 moles/hr. Since the condenser duty is slightly larger in high pressure column 22, the flow rate of partial stream 40 increases to about 56.70 moles/hr. Streams 40 and 56 are subsequently cooled in sub-cooler 42 to approximately -191.4°C before introduction in low pressure column 24. It is also to be noted that during such interval, oxygen enriched stream 30 flows at a rate of approximately 374.05 moles/hr. Stream 34 is diverted from one flow path to the other by turning turboexpander 76 and booster compressor 70 on and off. For instance, during the high demand phase, turboexpander 76 is shut off while compressor 70 is turned on. This causes the nitrogen rich vapour from stream 34 to divert itself from its use in supplying plant refrigeration, that is, its flow to turboexpander 76, to flow in main segment 18b of first pass 18a of main heat exchanger 18. The reverse operation occurs during the low demand phase. The foregoing method described above with reference to the drawing represents only one of many possible modes of plant operation in accordance with the present invention. For instance rather than on - off operation, turboexpander 76 could be set to vary the diverted flow rate in accordance with the level of demand, which might never cease during a particular demand pattern. During such a demand pattern, as demand for gaseous oxygen increased, turboexpander 76 could be controlled or regulated in a conventional manner to reduce steadily the flow of the nitrogen rich vapour therein so that anywhere from some to all of the nitrogen rich vapour would be available to be heated to about ambient temperature, compressed and condensed. At the same time, the flow of liquid nitrogen reflux would be increased with the decrease in the refrigeration being added to the process. As demand for gaseous oxygen decreased, turboexpander 76 could then be controlled to increase steadily the flow of the nitrogen rich vapour therein so that progressively less nitrogen rich vapour would be available to be heated to ambient temperature, compressed, and condensed. Concomitantly, the flow of liquid nitrogen reflux would be decreased with the increase of refrigeration being added to the process. The compressor 70 would also be operated continuously if there was a continuous demand for gaseous oxygen product.

Claims: A process for supplying gaseous oxygen to meet the requirements of a variable demand pattern including the steps of: a) continuously separating air into oxygen and nitrogen in a double rectification column comprising a higher pressure rectification column operatively associated with a lower pressure rectification column; b) continuously withdrawing nitrogen and liquid oxygen streams from the lower pressure rectification column; c) continuously condensing nitrogen separated in the higher pressure column and using one part of the resulting condensate as reflux in the higher pressure rectification column and another part thereof as reflux in the lower pressure rectification column; and d) continuously withdrawing a stream of nitrogen vapour from the higher pressure rectification column; e) expanding with the performance of external work at least a part of the stream of nitrogen vapour taken from the higher pressure rectification column so as to meet refrigeration requirements of the process; and f) when a demand for the gaseous oxygen exists, (i) pumping a product stream taken from the withdrawn liquid oxygen to a delivery pressure, diverting a stream of at least some of the said withdrawn nitrogen vapour from upstream of the said work expansion, warming by heat exchange said diverted nitrogen vapour stream, compressing the thus warmed nitrogen vapour stream, and heat exchanging the compressed nitrogen stream with the pumped product stream so as to vaporise the product stream and condense the compressed nitrogen stream; (ii) flashing a stream of the condensate formed by step (f) (i) to produce a two phase flow of nitrogen containing liquid and vapour phases and separating the liquid and vapour phases from one another; (iii) employing a stream of said liquid phase to supplement the reflux in the lower pressure rectification column; and (iv) adding a stream of the said vapour phase to the diverted nitrogen vapour to increase production of the gaseous oxygen; wherein at least some excess liquid oxygen is stored during periods of relatively low oxygen demand, and said stored liquid oxygen is used to increase oxygen production during periods of relatively high oxygen demand, and the rates at which nitrogen is expanded in step (e) and nitrogen is condensed in step (f) are varied with changing oxygen demand. A process according to claim 1, in which the rate at which said condensed compressed nitrogen is employed to supplement the reflux in the lower pressure rectification column is varied with oxygen demand. A process according to claim 2, in which liquid oxygen is withdrawn from the lower pressure rectification column at a constant rate. A process according to claim 1, wherein: the liquid nitrogen stream is added to the low pressure column at a rate varying with the introduction of plant refrigeration such that the liquid oxygen is formed within the low pressure column at an essentially constant rate; and the nitrogen vapour and the liquid oxygen are withdrawn from the high and low pressure columns at essentially constant rates. A process according to claim 1 or claim 4, wherein the liquid nitrogen is flashed into a flash tank to separate the liquid and vapour phases from one another.

Inventors: KLIGYS VITO, MOSTELLO ROBERT A, KLIGYS, VITO, MOSTELLO, ROBERT A.
Applicants: BOC GROUP INC, THE BOC GROUP, INC.
Application year: 1992
Main classification: F25J3
IPC codes: F25J3