VSA adsorption process

Abstract: A process for separating a feed gas mixture into a more strongly adsorbable component and a less strongly adsorbable component in a plurality of adsorbent beds containing an adsorbent selective for the more strongly adsorbable component using cocurrent depressurization to provide purge gas and pressurization by product end to product end pressure equalization between beds simultaneous with cocurrent ambient and elevated pressure feed pressurization, and countercurrent evacuation. Oxygen product can be recovered from air at high recovery and adsorbent productivity levels using the process.

Description: The present invention is directed to a pressure swing adsorption process for the separation of a more strongly adsorbable component from a less strongly adsorbable component in a gas mixture with high recovery of the less strongly adsorbable component at approximately feed pressure. More specifically, the present invention is a vacuum swing adsorption process for the separation of air to recover oxygen as a relatively unadsorbed product at high recovery and approximately feed pressure. Oxygen is a commodity chemical in the industrial gas industry. It has numerous applications including waste water treatment, glass melting furnaces, and the steel industry. One of the most common methods of oxygen production is by cryogenic distillation of air. However, this technology is not competitive for small size oxygen plants (<100 TPD O 2 ). The technology of choice for this size range is adsorption. There is a need in the marketplace to produce oxygen at low capital and energy costs by adsorptive gas separation. Adsorptive processes are extensively used in the industry to produce oxygen from air for small size oxygen plants (<100 TPD O 2 ). There are two major categories of these processes - pressure swing adsorption processes (PSA) and vacuum swing adsorption processes (VSA). The pressure swing adsorption processes carry out the adsorption (feed) step at pressures much higher than ambient and adsorbent regeneration at pressures close to ambient. The adsorbent beds go through secondary process steps, such as pressure equalizations, depressurizations, blowdowns, and purge or various combinations of these during the cycle. These processes tend to be energy intensive and more suitable for smaller oxygen plants producing less than 40 tons of oxygen per day and preferably less than 20 tons of oxygen per day. A subset of O 2 PSA processes is a rapid pressure swing adsorption (RPSA) process. As the name implies, this process involves similar steps as a PSA process, but carries out these steps very quickly. Again, this process tends to be energy intensive and suitable for oxygen plants even smaller than O 2 PSA's. Primary reasons for high energy consumption in PSA processes are: (1) O 2 recovery from these processes is low, and (2) the entire feed stream has to be compressed up to the adsorption pressure. These inefficiencies are somewhat circumvented in vacuum swing adsorption (VSA) processes. In these processes, adsorption is carried out at pressure slightly above ambient and adsorbent regeneration is carried out at sub-atmospheric levels. The adsorbent beds go through several secondary steps with the primary aim of increasing oxygen recovery and reducing adsorbent inventory per unit of product gas. U.S. Patent 4,917,710 describes a two bed O 2 VSA process with a product storage vessel. Process cycle steps are: adsorption, cocurrent depressurization, simultaneous cocurrent depressurization and evacuation, evacuation, vacuum purge by product, vacuum purge by gas obtained in a cocurrent depressurization step, simultaneous pressure equalization and product repressurization, and simultaneous feed and product repressurization. Gas for product repressurization and product purge is obtained from the product storage vessel. Gas for pressure equalization is obtained from the bed on simultaneous cocurrent depressurization and evacuation step. U.S. Patent 4,781,735 describes a three bed O 2 VSA process with steps: adsorption, feed to feed or dual end pressure equalization, cocurrent depressurization, evacuation, vacuum purge by gas obtained in cocurrent depressurization step, product repressurization from bed on feed step, simultaneous feed repressurization and feed to feed or dual end pressure equalization. European patent application 0 354 259 outlines various options for a two bed O 2 VSA process: adsorption, cocurrent depressurization, evacuation, pressure equalization with gas obtained in cocurrent depressurization step and feed repressurization. An option includes vacuum purge by product gas from the bed on adsorption step. U.S. Patent 5,015,271 describes an O 2 VSA process with the steps: adsorption, simultaneous cocurrent depressurization and countercurrent evacuation or feed, countercurrent evacuation, simultaneous product to product pressure equalization and feed repressurization, or vacuum purge, simultaneous feed and product repressurization and feed repressurization. U.S. Patent 5,122,164 describes an O 2 VSA process with the steps: adsorption, simultaneous cocurrent depressurization and countercurrent evacuation, countercurrent evacuation, vacuum purge, pressure equalization with gas from a bed undergoing cocurrent depressurization and product repressurization. U.S. Patent 5,223,004 describes an O 2 VSA process with the steps: adsorption, simultaneous cocurrent depressurization and countercurrent evacuation, countercurrent evacuation, purge, repressurization with product and cocurrent depressurization gas from another bed and repressurization with product and feed. U.S. Patent 5,328,503 (corresponding to EP-A-0 598 321) describes an O 2 VSA process with the steps: adsorption, cocurrent depressurization, simultaneous cocurrent depressurization and evacuation, evacuation, vacuum purge by gas obtained from the cocurrent depressurization step, pressure equalization with gas obtained from the simultaneous cocurrent depressurization step, and repressurization using various combinations of feed gas, product gas and ambient air. U.S. Patent 5,429,666 describes a two bed O 2 VSA process with the steps: adsorption, simultaneous cocurrent depressurization and evacuation, evacuation, vacuum purge by product gas, simultaneous pressure equalization and repressurization using cocurrent depressurization gas and feed gas/ambient air respectively, and repressurization using various combinations of feed gas, product gas and ambient air. Despite the prior art, a need still exists for an O 2 VSA process with higher oxygen recovery (i.e. lower energy costs) and lower adsorbent requirement per unit of oxygen production (i.e. lower capital costs) than the current processes. The present invention outlines a vacuum swing adsorption (VSA) process to produce oxygen from air at higher oxygen recovery and lower adsorbent requirement per unit of oxygen product than current O 2 VSA processes. The present invention is a process for selectively separating a more strongly adsorbable component from a less strongly adsorbable component of a feed gas mixture in a plurality of adsorption beds containing an adsorbent selective for the more strongly adsorbable component, according to claim 1. The subclaims define advantageous embodiments of the invention. The drawing is a schematic drawing of a preferred embodiment of the present invention using two parallel adsorption beds and appropriate valve manifolding for feed, evacuation, purge, equalization and repressurization. The present invention will now be described with regard to a preferred embodiment. The preferred embodiment has the following steps: 1. Adsorption (A) to provide product, 2. Cocurrent depressurization (DP1) to provide purge to a bed undergoing countercurrent vacuum purge, 3. Cocurrent depressurization (DP2) to provide pressure equalization gas and simultaneous initiation of countercurrent evacuation, 4. Countercurrent evacuation (DES), 5. Countercurrent vacuum purge (PU) with cocurrent depressurization gas from (DP1), 6. Pressure equalization (PE) with cocurrent depressurization gas from (DP2) and repressurization with ambient pressure feed gas and elevated pressure feed gas. 7. Feed repressurization (RP) with elevated pressure feed gas, or combinations with ambient pressure feed gas. A process cycle chart for this option is outlined in Table 1. Process steps for the preferred embodiment will now be described in detail: 1. Adsorption Step (A) , which comprises: a. Flowing the elevated feed gas mixture, exemplified by atmospheric air at a pressure of 1,03-2,07 bar (15-30 psia) and temperature of ∼-17,8-65,6 ° C (∼0-150°F) through a bed packed with one or more adsorbents capable of selectively adsorbing water, carbon dioxide, and nitrogen from air. b. Withdrawing an effluent stream consisting of O 2 product at feed pressure. c. Continuing steps 1(a) and 1(b) for a predetermined cycle time or until the concentration of nitrogen impurity in the effluent stream reaches a preset limit. The bed is now called "spent" because it has exhausted its capacity for removing nitrogen from feed gas. 2. Cocurrent Depressurization Step (DP1) , which comprises: a. Discontinuing the feed flow through the spent bed and transferring the feed to another VSA bed. b. Reducing the pressure in the spent VSA bed from the adsorption pressure level to some "intermediate" level (0,69-1,72 bar (10-25 psia)) by connecting the product end of this bed with the product end of the VSA bed on step 5 of its cycle. c. Discontinuing the above step when the pressure in the spent VSA bed has reached the predetermined intermediate pressure level. 3. Cocurrent Depressurization Step (DP2) , which comprises: a. Reducing the pressure in the spent VSA bed from the intermediate pressure level to some "lower" level (0,53-1,39 bar (7.7-20 psia)) by connecting the product end of this bed with the product end of the VSA bed on step 6 of its cycle while simultaneously initiating countercurrent evacuation of the spent VSA bed. b. Discontinuing the above step when the pressure in the spent VSA bed has reached the predetermined lower pressure level. 4. Countercurrent Evacuation Step (DES) , which comprises: a. Further reducing the pressure in the spent bed from lower level to the "lowest" level (0,07-0,69 bar (1.0-10.0 psia)) by connecting the feed end of the spent VSA bed with a source of vacuum, such as a vacuum pump. b. Continuing the above step until the pressure in the VSA bed has reached the predetermined lowest pressure level. 5. Countercurrent Purge Step (PU) , which consists of: a. Continuing evacuation of the VSA bed from the feed end. b. Connecting the product end of this bed with another VSA bed on step 2 of its cycle. c. Continuing the above steps until pressure in this bed has reached a "low" level (0,07-0,83 bar (1-12 psia)). 6. Pressure Equalization Step (PE) , which consists of: a. Discontinuing evacuation of the above bed and start evacuating another VSA bed. This bed is now called "regenerated" since its capacity for more strongly adsorbed components, such as N 2 , H 2 O, and CO 2 removal from air, has been restored. b. Connecting the product end of the regenerated bed with the product end of the bed on step 3 of its cycle and connecting the feed end of the bed with ambient pressure feed gas mixture and elevated pressure feed gas mixture. c. Continuing the above step for a predetermined time or until pressure in the regenerated bed has reached the predetermined lower level. At the end of PE, step 6, the two beds are much closer in pressure; such that the pressure difference between the two beds is generally less than 0,1379 bar (2 psia), and preferably less than 0,0689 bar (1 psia). 7. Repressurization Step , which consists of: a. Discontinuing the pressure equalization of regenerated bed. A. Repressurization (RP) , which consists of: i) Connecting the feed end of the pressure equalized regenerated bed with the elevated pressure feed gas mixture and potentially with ambient pressure feed gas mixture. ii) Continuing the above step until pressure in the regenerated bed is close to or equal to the predetermined adsorption pressure. OR B. Simultaneous Product and Feed Repressurization Step (PRP/FRP) , which consists of: i) Connecting the product end of the regenerated bed with the product reservoir and opening the feed end of the regenerated bed to the feed blower and potentially to ambient pressure feed gas mixture. ii) Continuing the above step until the pressure in the regenerated bed is equal to the predetermined adsorption pressure. OR C. Sequential Product and Feed Repressurization Step (PRP/FRP) , which consists of: i) Connecting the product end of the regenerated bed with a product reservoir. ii) Discontinuing the product repressurization and opening the feed end of the regenerated bed to the feed blower and potentially to ambient pressure feed gas mixture. iii) Continuing the above step until the pressure in the regenerated bed is equal to the predetermined adsorption pressure. OR D. Sequential Feed and Product Repressurization , which consists of: i) Connecting the feed end of the regenerated pressure equalized bed to the feed blower and potentially to ambient pressure feed gas mixture. ii) Continuing the above feed repressurization step until pressure in the regenerated bed has reached the predetermined pressure level, which is lower than the adsorption pressure. iii) Discontinuing the feed repressurization step and connecting the product end of the regenerated bed with a product reservoir. iv) Continuing the above step until the pressure in the regenerated bed is equal to the predetermined adsorption pressure. The bed is now ready to undergo a new cycle starting from step 1(a). Flow schematic and hardware will be somewhat different for each of the process options of the present invention. The drawing depicts a schematic for the first preferred embodiment with feed and ambient air repressurization. Table 2 outlines the corresponding valve sequence for a typical cycle time. Detailed process description of the cycle at typical operating conditions for the process option described in the drawing and Tables 1 and 2 is given below: Ambient air compressed to feed pressure (1,45 bar (21 psia)) by a feed blower 111 comprises the elevated feed gas mixture and enters through manifold 100 and open valve 1 into first Bed A, which has already been pressurized to adsorption pressure. The Bed is packed with adsorbent(s) selective for the removal of water, carbon dioxide, and nitrogen from air. Oxygen product is withdrawn via open valve 8 and manifold 104 to product reservoir 109. Feed flow is discontinued after a predetermined time or as soon as nitrogen concentration in the effluent from Bed A reaches a preset limit or the adsorption front approaches the bed outlet. Pressure in Bed A is reduced by closing valve 8 and opening valve 6 and connecting Bed A with Bed B via manifold 106, to provide purge gas for Bed B. Valve 5 also opens during this step, to vent feed gas out manifold 103. Pressure in Bed A is further reduced by closing valve 6 and opening valve 7 and connecting Bed A with Bed B via manifold 107. Bed A is simultaneously evacuated via open valve 2 and manifold 102 by a source of vacuum, such as vacuum pump 110. Valve 7 is closed and valve 2 remains opened until Bed A reaches an evacuation level pressure -0,28 bar (∼4 psia) in Bed A. Valve 2 is kept open for a predetermined time while valve 6 is opened to vacuum purge Bed A through manifold 106 with provide purge gas from Bed B. Valves 2 and 6 are then closed and valves 1, 5 and 7 are opened for simultaneous ambient feed gas mixture (air), elevated pressure feed air and Bed B cocurrent depressurization gas repressurization through manifolds 103, 100 and 107, respectively. Valve 5 is kept open until pressure in Bed A reaches ambient pressure. At this time, valve 5 is closed and bed A is now pressurized up to adsorption pressure -1,45 bar (-21 psia) with elevated pressure feed air from manifold 100. Valve 8 is opened to remove product oxygen through manifold 104. Bed A is now ready to start a new cycle. Both beds go through a similar sequence of operation but out of phase with one another. The vacuum pump 110 runs continuously, allowing simplification of operation and downsizing of that equipment. Valve Sequence: 2 Bed Oxygen VSA Valve # --> Time (sec) 1 2 3 4 5 6 7 8 9 0-5 o o o o 5-15 o o o 15-35 o o o 35-40 o o o 40-45 o o o o 45-55 o o o 55-75 o o o 75-80 o o o o = open, otherwise closed Any adsorbent(s) which can selectively separate more strongly adsorbed components from less strongly adsorbed components of a particular feed gas mixture can be used, and the evaluation of such adsorbents for a particular feed gas mixture is well within the capability of those skilled in the art. In the preferred embodiment, an adsorbent that selectively removes water, carbon dioxide, and nitrogen from air can be used. Examples of adsorbents capable of removing nitrogen from air include zeolitic molecular sieves such as NaX, NaA, CaX, CaA and other adsorbents with binary cations. Examples of adsorbents capable of removing water and carbon dioxide from air are aluminas, silica gels and zeolites. Other desired properties of the adsorbents are (i) high crush strength, (ii) high attrition resistance, (iii) large bulk density, (iv) low interpartical void, (v) high heat capacity, (vi) large thermal conductivity, (vii) high N 2 /O 2 selectivity, (viii) low oxygen capacity and (ix) small particle size. Pressure drop through the adsorbent beds during adsorption and evacuation steps is also important for adsorbent selection. The benefit of the Present Invention over an oxygen VSA process that does not have the features of the Present Invention, such as cocurrent depressurization for purge, can be seen in the comparison of the Present Invention and U.S. 5,429,666, which were both run in a pilot development unit with the following parameters set for each process. Process Conditions Product Purity = 90% O 2 Feed Pressure = 1,41 bar (20.4 psia) Evacuation Pressure = 0,32 bar (4.7 psia) Feed Temperature -- Ambient Maximum approach to adsorbent fluidization dP while providing cocurrent pressure equalization/purge gas = 80% Adsorbents - NaX at the feed end followed by CaX zeolite Length = 2,13 m (7 ft) Diameter = 0,91 m (3 ft) Cycle Time = 88 sec. The results of this comparative test is set forth in Table 3 below which shows a lower adsorbent requirement, higher recovery and lower feed blower and vacuum pump sizes, resulting in a lower cost for oxygen in the Present Invention. U.S. 5,429,666 Present Invention O 2 Recovery (%) 42 47 lb Adsorbent/TPDC 1 0.97 Feed Blower ACFM /TPDC 1 0.95 Vacuum Blower ACFM/TPDC 1 0.95 Power Consumption 1 1 Oxygen Cost 1 0.97 The present invention achieves this desirable lower cost of producing product, such as oxygen, in an adsorptive separation by recovering a greater percentage of the oxygen contained in the feed gas. In the process described by U.S. 5,429,666, the optimal amount of pressure equalization gas may not be exchanged between the two adsorbers, if the rate of gas exchanged has to be restricted in order to prevent upward fluidization of the adsorbent in the adsorber providing this gas. If the optimum amount of pressure equalization gas is not exchanged, the bed providing gas still contains a significant quantity of oxygen in its void spaces at the end of the provide pressure equalization step. This oxygen is then removed (lost) through the vacuum pump on the subsequent evacuation step. The present invention improves recovery by employing two cocurrent desorption steps (provide purge and pressure equalization) instead of one. Approximately twice as much void space oxygen can be passed from one adsorber to another, without risk of fluidizing the adsorbent, before evacuation starts. The inefficiency associated with idling the feed blower during the provide purge step is more than compensated for by the higher oxygen recovery.

Claims: A process for selectively separating a more strongly adsorbable component from a less strongly adsorbable component of a feed gas mixture in a plurality of adsorption beds containing an adsorbent selective for the more strongly adsorbable component, comprising the steps of: (a) introducing a feed gas mixture at elevated pressure containing said more strongly adsorbable component and said less strongly adsorbable component into an inlet of a first adsorption bed containing said adsorbent selective for the more strongly adsorbable component and adsorbing the more strongly adsorbable component on the adsorbent while the less strongly adsorbable component passes through said first bed unadsorbed as a product and continuing until the adsorption front of said more strongly adsorbable component approaches an outlet of said first bed and terminating the introduction of said feed gas mixture; (b) cocurrently depressurizing said first bed to remove a cocurrent depressurization gas from said first bed and passing said cocurrent depressurization gas to an outlet of a bed undergoing purging of step (e); (c) further cocurrently depressurizing said first bed to a lower pressure to remove additional cocurrent depressurization gas from said first bed and passing said additional cocurrent depressurization gas to an outlet of a bed of said plurality of adsorption beds at lower pressure undergoing repressurizing of step (f) to at least partially pressure equalize the two beds, while countercurrently depressurizing said first bed by connection to a source of vacuum; (d) countercurrently evacuating said first bed under vacuum conditions to remove said more strongly adsorbable component; (e) countercurrently purging said first bed with said cocurrent depressurization gas from a bed of said plurality of adsorption beds undergoing step (b) to remove additional more strongly adsorbable component from said first bed; (f) repressurizing said first bed with ambient pressure feed gas mixture, elevated pressure feed gas mixture and, simultaneously, with said cocurrent depressurization gas from a bed of said plurality of adsorption beds undergoing the cocurrent depressurization of step (c); (g) further repressurizing said first bed with elevated pressure feed gas mixture; and (h) performing steps (a) through (g) in each of said plurality of adsorption beds in a phased sequence. The process of claim 1 wherein in step (b) said first bed is depressurized to an intermediate pressure. The process of Claim 1 or 2 wherein said bed is repressurized in step (g) with ambient pressure feed gas mixture and elevated pressure feed gas mixture. The process of Claim 1 or 2 wherein said bed is repressurized in step (g) initially with feed gas mixture and then with less strongly adsorbable component. The process of Claim 1 or 2 wherein said bed is repressurized in step (g) initially with less strongly adsorbable component and then with feed gas mixture. The process of Claim 1 or 2 wherein said bed is repressurized in step (g) with less strongly adsorbable component and feed gas mixture simultaneously. The process of one of the Claims 1 to 6 wherein said feed gas mixture is air, said more strongly adsorbable component is nitrogen and said less strongly adsorbable component is oxygen. The process of Claim 7 wherein the process is carried out in two beds. The process of one of the Claims 1 to 8 wherein the pressure equalization of step (c) is a complete pressure equalization. The process of one of the Claims 7, 8 or 9 wherein said elevated pressure feed air is at a pressure in the range of approximately 1,03-2,07 bar (15-30 psia). The process of Claim 10 wherein said elevated pressure feed air is at a pressure in the range of approximately 1,03-1,66 (15-24 psia). The process of one of the Claims 7 to 11 wherein at the end of said countercurrent evacuation of step (d) said bed is at a pressure in the range of approximately 0,069-0,689 bar (1-10 psia).

Inventors: AGRAWAL RAKESH, KUMAR RAVI, NAHEIRI TARIK, WATSON CHARLES FRANKLIN, AGRAWAL, RAKESH, KUMAR, RAVI, NAHEIRI, TARIK, WATSON, CHARLES FRANKLIN
Applicants: AIR PROD & CHEM, AIR PRODUCTS AND CHEMICALS, INC.
Application year: 1996
Main classification: B01D53
IPC codes: B01D53