METHOD FOR THE PRODUCTION OF AIR GASES BY THE CRYOGENIC SEPARATION OF AIR

Abstract

A method for the production of air gases by the cryogenic separation of air can include the steps of sending a purified and compressed air stream to a cold box under conditions effective for cryogenically separating the air stream into an oxygen product and nitrogen using a system of columns, wherein the purified and compressed air stream is at a feed pressure when entering the system of columns; withdrawing the oxygen product at a product pressure; delivering the oxygen product at a delivery pressure to an oxygen pipeline, wherein the oxygen pipeline has a pipeline pressure; wherein during the second mode of operation, the method can include monitoring the pipeline pressure; and reducing the difference between the pipeline pressure and the delivery pressure. By operating the method in a dynamic fashion, a power savings can be realized in instances in which the pipeline pressure deviates from its highest value.

Claims

1. A method for the production of air gases by the cryogenic separation of air, the method comprising the steps of: a) compressing air to a pressure suitable for the cryogenic rectification of air to produce a compressed humid air stream, the compressed humid air stream having a first pressure P.sub.o; b) purifying the compressed humid air stream of water and carbon dioxide within a front end purification system to produce a dry air stream having reduced amounts of water and carbon dioxide as compared to the compressed humid air stream; c) compressing a first portion of the dry air stream in a booster compressor to form a boosted air stream, the boosted air stream having a first boosted pressure P.sub.B1; d) introducing a second portion of the dry air stream and the boosted air stream to a cold box under conditions effective to separate air to form an air gas product, wherein the air gas product is selected from the group consisting of oxygen, nitrogen, and combinations thereof; e) withdrawing the air gas product from the cold box, the air gas product having a first product pressure P.sub.P1; f) introducing the air gas product to a pipeline, wherein the pipeline is configured to transport the air gas product to a location located downstream of the pipeline, wherein the pipeline operates at a pipeline pressure P.sub.PL, wherein the air gas product is introduced to the pipeline at a first delivery pressure P.sub.D1; g) monitoring the pipeline pressure P.sub.PL within the pipeline; and h) adjusting one or more pressure set points within the cold box based on the pipeline pressure P.sub.PL.

2. The method as claimed in claim 1, wherein the one or more pressure set points of step h) is the first product pressure P.sub.P1.

3. The method as claimed in claim 1, wherein the first boosted pressure P.sub.B1 is adjusted such that the difference between the first delivery pressure P.sub.D1 and the pipeline pressure P.sub.PL is below a given threshold.

4. The method as claimed in claim 3, wherein the threshold is less than 5 psi.

5. The method as claimed in claim 3, wherein the threshold is less than 3 psi.

6. The method as claimed in claim 1, wherein the cold box comprises a main heat exchanger, a system of columns having a double column composed of a lower pressure column and a higher pressure column, a condenser disposed at a bottom portion of the lower pressure column, and a liquid oxygen pump.

7. The method as claimed in claim 6, wherein the air gas product is oxygen and the pipeline is an oxygen pipeline.

8. The method as claimed in claim 7, wherein the liquid oxygen pump pressurizes liquid oxygen from the lower pressure column to the first product pressure P.sub.P1.

9. The method as claimed in claim 1, wherein the first product pressure P.sub.P1 is adjusted based upon the monitored pipeline pressure P.sub.PL.

10. The method as claimed in claim 9, wherein the first boosted pressure P.sub.B1 is adjusted based upon the first product pressure P.sub.P1.

11. The method as claimed in claim 6, wherein the air gas product is nitrogen and the pipeline is a nitrogen pipeline.

12. A method for the production of air gases by the cryogenic separation of air, the method comprising a first mode of operation and a second mode of operation, wherein during the first mode of operation and the second mode of operation, the method comprises the steps of: sending a purified and compressed air stream to a cold box under conditions effective for cryogenically separating the air stream to form an air gas product using a system of columns, wherein the purified and compressed air stream is at a feed pressure P.sub.F when entering the cold box, wherein the air gas product is selected from the group consisting of oxygen, nitrogen, and combinations thereof; withdrawing the air gas product at a product pressure P.sub.PO; delivering the air gas product at a delivery pressure P.sub.DO to an air gas pipeline, wherein the air gas pipeline has a pipeline pressure P.sub.PL; wherein during the second mode of operation, the method further comprises the steps of: monitoring the pipeline pressure P.sub.PL; and reducing the difference between the pipeline pressure P.sub.PL and the delivery pressure P.sub.DO.

13. The method as claimed in claim 12, wherein the step of reducing difference between the pipeline pressure P.sub.PL and the delivery pressure P.sub.DO further comprises adjusting the product pressure P.sub.PO.

14. The method as claimed in claim 13, wherein the step of reducing difference between the pipeline pressure P.sub.PL and the delivery pressure P.sub.DO further comprises the step of adjusting the feed pressure P.sub.F.

15. The method as claimed in claim 12, wherein the product pressure P.sub.PO and the delivery pressure P.sub.DO are substantially the same.

16. The method as claimed in claim 12, wherein the air gas product is oxygen, wherein the cold box comprises a main heat exchanger, a system of columns having a double column composed of a lower pressure column and a higher pressure column, a condenser disposed at a bottom portion of the lower pressure column, and a liquid oxygen pump.

17. The method as claimed in claim 16, wherein the cold box further comprises a gaseous oxygen (GOX) feed valve, wherein the GOX feed valve is in fluid communication with an outlet of the liquid oxygen pump and an inlet of the air gas pipeline.

18. The method as claimed in claim 17, wherein the step of reducing the difference between the pipeline pressure P.sub.PL and the delivery pressure P.sub.DO comprises an absence of adjusting the GOX feed valve.

19. The method as claimed in claim 17, wherein the step of reducing the difference between the pipeline pressure P.sub.PL and the delivery pressure P.sub.DO includes maintaining the GOX feed valve fully open.

20. The method as claimed in claim 16, further comprising the step of providing a main air compressor upstream the cold box, wherein the step of reducing difference between the pipeline pressure P.sub.PL and the delivery pressure P.sub.DO further comprises the step of adjusting the operation of the liquid oxygen pump and the operation of the main air compressor, such that the product pressure P.sub.PO and the feed pressure P.sub.F are adjusted.

21. The method as claimed in claim 16, further comprising the step of providing a booster compressor downstream a main air compressor and upstream the cold box, wherein the step of reducing difference between the pipeline pressure P.sub.PL and the delivery pressure P.sub.DO further comprises the step of adjusting the operation of the liquid oxygen pump and the operation of the booster compressor, such that the product pressure P.sub.PO and the feed pressure P.sub.F are adjusted.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0070] These and other features, aspects, and advantages of the present invention will become better understood with regard to the following description, claims, and accompanying drawings. It is to be noted, however, that the drawings illustrate only several embodiments of the invention and are therefore not to be considered limiting of the invention's scope as it can admit to other equally effective embodiments.

[0071] FIG. 1 provides an embodiment of the present invention.

[0072] FIG. 2 provides another embodiment of the present invention.

[0073] FIG. 3 provides a graphical representation of data for an embodiment of the present invention.

DETAILED DESCRIPTION

[0074] While the invention will be described in connection with several embodiments, it will be understood that it is not intended to limit the invention to those embodiments. On the contrary, it is intended to cover all the alternatives, modifications and equivalence as may be included within the spirit and scope of the invention defined by the appended claims.

[0075] Now turning to FIG. 1. Air 2 is introduced into main air compressor 10 and compressed, preferably to a pressure of at least 55 psig to 75 psig (or around 5 psig higher than the pressure of the higher pressure column). The resulting compressed humid air stream 12 is then purified of water and CO.sub.2 in front end purification system 20, thereby producing dry air stream 22. In one embodiment, all of dry air stream 22 passes via line 26 into cold box 40. The pressure of dry air stream 22 is measured by first pressure indicator PI1a. Within cold box 40, the air is cooled and cryogenically treated in order to separate the air into air gas product 42. Air gas product 42 is then removed from cold box 40 and passed through product control valve 50 before entering air gas pipeline 60. In a preferred embodiment, the pressure and flow rate of air gas product 42 can be measured by second pressure indicator PI2 and flow indicator FI1, respectively. The pressure of air gas pipeline 60 can be measured by pressure indicator PI3.

[0076] In one embodiment, the various pressure and flow indicators/sensors are configured to communicate (e.g., wirelessly or wired communication) with process controller 55, such that the various flow rates and pressures can be monitored by process controller 55, which is configured to adjust various settings throughout the process based on the measured flows and pressures.

[0077] Additionally, an embodiment of the present invention may also include booster air compressor 30. This embodiment is represented by dashed lines, since it is an optional embodiment. In this embodiment, a portion of dry air stream 22 is sent to booster air compressor 30 via line 24 and further compressed to form boosted air stream 32 before being introduced to cold box 40. The addition of booster air compressor 30 allows for additional freedoms in fine tuning the process, as will be explained in more detail later. In this embodiment, first pressure indicator PI1b is located on line 32 instead of line 26. Similarly, pressure controller 14b is in communication with booster air compressor 30 as opposed to pressure controller 14a for main air compressor 10. While the embodiment of FIG. 1 shows booster air compressor 30 as a single compressor, those of ordinary skill in the art will recognize that booster air compressor 30 can be more than one physical compressor. Additionally, booster air compressor 30 can also be a multi-stage compressor.

[0078] While the figures show direct lines of communication from the various pressure and flow indicators to the process controller 55, embodiments of the invention should not be so limited. Rather, those of ordinary skill in the art will recognize that embodiments of the invention may include instances in which certain indicators communicate directly with a related pressure controller.

[0079] FIG. 2 provides a more detailed view of cold box 40 for the optional embodiment that includes booster air compressor 30. In this embodiment, cold box 40 also includes heat exchanger 80, turbine 90, valve 100, double column 110, higher pressure column 120, auxiliary heat exchanger 130, lower pressure column 140, condenser/reboiler 150, and liquid oxygen pump 160. Turbine 90 can be attached to booster 70 via a common shaft. Just like in FIG. 1, air 2 is introduced into main air compressor 10 and compressed, preferably to a pressure of at least 55 psig to 75 psig (or around 5 psig higher than the pressure of the higher pressure column). The resulting compressed humid air stream 12 is then purified of water and CO.sub.2 in front end purification system 20, thereby producing dry air stream 22. A first portion of dry air stream 24 is sent to booster air compressor 30, with the remaining portion of dry air stream 26 entering cold box 40, wherein it is fully cooled in heat exchanger 80 before being introduced to higher pressure column 120 for separation therein. Following pressurization in booster air compressor 30, boosted air stream 32 is preferably fully cooled in heat exchanger 80 and then expanded across valve 100, before being introduced into a bottom portion of higher pressure column 120.

[0080] Partially boosted air stream 37 is preferably removed from an inner stage of booster air compressor 30 before being further compressed in booster 70 and then cooled in after cooler 75 to form second boosted stream 72. Second boosted stream 72 undergoes partial cooling in heat exchanger 80, wherein it is withdrawn from an intermediate section of heat exchanger 80 and then expanded in turbine 90 thereby forming expanded air stream 92, which can then be combined with second portion of dry air stream 26 before introduction to higher pressure column 120.

[0081] Higher pressure column 120 is configured to allow for rectification of air within, thereby producing an oxygen-rich liquid at the bottom and a nitrogen-rich gaseous stream at the top. Oxygen-rich liquid 122 is withdrawn from the bottom of higher pressure column 120 before exchanging heat with low pressure waste nitrogen 114 and low pressure nitrogen product 112 in auxiliary heat exchanger 130, and then expanded across a valve and introduced into lower pressure column 140. As is well known in the art, higher pressure column 120 and lower pressure column 140 are part of double column 110, and the two columns are thermally coupled via condenser/reboiler 150, which condenses rising nitrogen rich gas from higher pressure column 120 and vaporizes liquid oxygen that has collected at the bottom of lower pressure column 140. In the embodiment shown, two nitrogen-rich liquid streams 126, 128 are withdrawn from higher pressure column 120, exchange heat with low pressure nitrogen product 112 and low pressure waste nitrogen 114, subsequently expanded across their respective valves, and then introduced into lower pressure column 140. Higher pressure nitrogen product 129 can also be withdrawn from higher pressure column 120 and then warmed in heat exchanger 80.

[0082] Liquid oxygen collects at the bottom of lower pressure column 140 and is withdrawn and pressurized to an appropriate pressure by liquid oxygen pump 160 to form liquid oxygen product 162. Liquid oxygen product 162 is then vaporized within heat exchanger 80 to form air gas product 42. The pressure and flow rate of air gas product 42 can be measured via second pressure sensor PI2 and FI1, respectively. As in FIG. 1, air gas product 42 flows across product control valve 50 and into air gas pipeline 60.

[0083] As noted previously, the pressure of air gas pipeline 60 tends to drift over time. In methods known heretofore, this problem was solved by adjusting the openness of product control valve 50 to create the appropriate pressure drop. However, there are inefficiencies in doing this. Instead, embodiments of the present invention can adjust the pressure set points within the cold box, for example, the discharge pressure of liquid oxygen pump 160. By reducing this pressure an appropriate amount, product control valve 50 can be left fully open, thereby resulting in minimal expansion losses across product control valve 50. In one embodiment, the appropriate amount yields a difference between PI2 and PI3 to be less than 5 psi, preferably less than 3 psi.

[0084] In another embodiment, by changing the pressure of liquid oxygen product 162, its vaporization temperature will also change. Furthermore, it is preferred that liquid oxygen product 162 vaporizes against a condensing air stream (e.g., boosted air stream 32). As such, in a preferred embodiment, the discharge pressure of booster air compressor 30 is also changed an appropriate amount. In one embodiment, an appropriate amount is preferably the amount that results in improved heating curves between liquid oxygen product 162 and boosted air stream 32.

[0085] In an embodiment in which the air gas product is nitrogen, the embodiment may include withdrawing higher pressure nitrogen product 129 as a liquid from higher pressure column 120, and pressurizing it to an appropriate pressure using a liquid nitrogen pump (not shown) before warming in heat exchanger 80. The resultant warmed nitrogen gas product would then be introduced to a nitrogen pipeline in similar manner as described with respect to the gaseous oxygen product. Alternatively, a liquid nitrogen stream can be removed from the lower pressure column instead of the higher pressure column.

[0086] FIG. 3 provides a graphical representation of pressures as a function of time for an embodiment of the present invention. As can be seen from FIG. 3, the ASU GOX pressure is kept slightly above (e.g., between 3-4 psi) the GOX pipeline pressure. This is accomplished by altering both the LOX discharge pressure from the LOX pump, as well as altering the booster air compressor (BAC) discharge pressure. By operating the LOX pump and BAC in variable speed mode, embodiments of the present invention are able to save on power consumption without any losses in flow rate production, and therefore, present an incredible advantage over the methods known heretofore.

[0087] Table I and Table II below, show comparative data of the various streams for oxygen production at 610 psig and 400 psig.

TABLE-US-00001 TABLE I 610 psig GOX Flow Pressure Temp Stream # (kscfh) (psig) (° F.) 2 7430 0 72 12 7430 71 87 24 3200 69 64 26 4143 69 64 32 2188 966 87 37 1012 525 87 42 1413 615 69 72 1012 794 87 92 1012 66 −280 94 5155 66 −260.5 162 1413 620 −287 MP Col — 66 — LP Col — 6 —

TABLE-US-00002 TABLE II 400 psig GOX Flow Pressure Temp Stream # (kscfh) (psig) (° F.) 2 7430 0 72 12 7430 71 87 24 3200 69 64 26 4143 69 64 32 2188 929 87 37 1012 513 87 42 1413 405 71 72 1012 794 87 92 1012 66 −280 94 5155 66 −266.5 162 1413 409 −289 MP Col — 66 — LP Col — 6 —

[0088] As is shown in the tables above, when the pipeline pressure changes, the pressures of streams 32, 37, 42 and 162 can be adjusted, while maintaining all other conditions substantially the same. As will be readily appreciated, being able to reduce compression needs for the LOX pump 160 and BAC 30 can result in significant power savings. Furthermore, this is accomplished without any loss of production in terms of flow rate and without any significant upset to the operating conditions of the double column.

[0089] The terms “nitrogen-rich” and “oxygen-rich” will be understood by those skilled in the art to be in reference to the composition of air. As such, nitrogen-rich encompasses a fluid having a nitrogen content greater than that of air. Similarly, oxygen-rich encompasses a fluid having an oxygen content greater than that of air.

[0090] While the invention has been described in conjunction with specific embodiments thereof, it is evident that many alternatives, modifications, and variations will be apparent to those skilled in the art in light of the foregoing description. Accordingly, it is intended to embrace all such alternatives, modifications, and variations as fall within the spirit and broad scope of the appended claims. The present invention may suitably comprise, consist or consist essentially of the elements disclosed and may be practiced in the absence of an element not disclosed. Furthermore, if there is language referring to order, such as first and second, it should be understood in an exemplary sense and not in a limiting sense. For example, it can be recognized by those skilled in the art that certain steps can be combined into a single step.

[0091] The singular forms “a”, “an” and “the” include plural referents, unless the context clearly dictates otherwise.

[0092] “Comprising” in a claim is an open transitional term which means the subsequently identified claim elements are a nonexclusive listing (i.e., anything else may be additionally included and remain within the scope of “comprising”). “Comprising” as used herein may be replaced by the more limited transitional terms “consisting essentially of” and “consisting of” unless otherwise indicated herein.

[0093] “Providing” in a claim is defined to mean furnishing, supplying, making available, or preparing something. The step may be performed by any actor in the absence of express language in the claim to the contrary.

[0094] Optional or optionally means that the subsequently described event or circumstances may or may not occur. The description includes instances where the event or circumstance occurs and instances where it does not occur.

[0095] Ranges may be expressed herein as from about one particular value, and/or to about another particular value. When such a range is expressed, it is to be understood that another embodiment is from the one particular value and/or to the other particular value, along with all combinations within said range.

[0096] All references identified herein are each hereby incorporated by reference into this application in their entireties, as well as for the specific information for which each is cited.