Process for generating higher VPSA product pressure
The invention relates to a process for modifying the VPSA/VSA/PSA cycle to allow for maximum product pressure without the need for a base load oxygen compressor (BLOC) or base load oxygen blower (BLOB), thus supplying low pressure oxygen (3 to 7 Psig) to the end user while at the same time lowering product costs 10 to 30%. The system of this invention preferably employs larger piping runs from the VPSA to the oxy-fuel control skids, larger piping for the oxy-fuel control skid, larger piping for the VPSA, low pressure drop flow measurements, and low pressure drop check valves.
1. A pressure swing adsorption method for the separation of components of a feed gas mixture into at least a first component and a second component by selective adsorption of said first component into a bed of adsorbent, said method comprising the following steps on a cyclic basis:
a) raising the pressure of said feed gas to said bed during adsorption steps of the cycle to an adsorption pressure so as to enable adsorption of said first component by said adsorbent, said adsorbent exhibiting a mass transfer coefficient of >=12/s and an intrinsic N 2 diffusivity of equal to or greater than 4.0×10 −6 m 2 /sec at 27.55 psia and 300k,
b) depressurizing said bed during the desorption steps of said cycle to a desorption pressure so as to desorb said first component from said adsorbent, a ratio of pressures of said adsorption pressure to said desorption pressure ranging from about 1.5 to 3.5;
wherein said bed is pressurized to said adsorption pressure by pressurized feed gas and with no product pressurization.
2. The pressure swing adsorption method of claim 1 , wherein a lowest pressure during a cycle is from 6 to 12 psia and a highest pressure during said cycle is from within about 2 to 12 psig.
3. The pressure swing adsorption method of claim 1 , wherein said feed gas is air, said first component is nitrogen and said second component is oxygen.
4. The pressure swing adsorption method of claim 1 , wherein said adsorbent is a particulate having an average particle diameter of from about 0.8 mm to about 1.6 mm.
5. The pressure swing adsorption method of claim 1 , wherein said adsorbent is a type X zeolite with a SiO 2 /Al 2 O 3 ratio less than or equal to 2.5 and exchanged with Li (>70%).
6. The pressure swing adsorption method of claim 1 , wherein said bed of adsorbent has a dimension, in a direction of flow of said gas through said bed of adsorbent, of less than about 1.2 m and said method performs steps a) and b) in a time of less than about 40 seconds.
7. The pressure swing adsorption method of claim 1 , wherein said bed of adsorbent has a dimension, in a direction of flow of said gas through said bed of adsorbent, of less than about 0.9 m and said method performs steps a) and b) in a time of less than about 30 seconds.
8. The pressure swing adsorption method of claim 1 , wherein said bed of adsorbent has a dimension, in a direction of flow of said gas through said bed of adsorbent, of less than about 0.6 m and said method performs steps a) and b) in a time of less than about 20 seconds.
9. The pressure swing adsorption method of claim 1 , wherein said first component comprises N2 and said method is adapted for the recovery of O 2 from feed air in a purity range of >70% O 2.
10. A pressure swing adsorption system for separating components of a feed gas mixture into at least a first component and a second component by selective adsorption of said first component into a bed of adsorbent particles during the adsorption steps of the cycle, said system comprising at least two adsorption vessels each containing a bed of adsorbent material that is selective for said first component, said adsorbent exhibiting an intrinsic diffusivity for said first component that is equal to or greater than 4.0×10 −6 m 2 /sec at 27.55 psia and 300k, said system configured to raise the pressure of said feed gas to the bed of adsorbent particles during adsorption steps of the cycle to an adsorption pressure so as to enable adsorption of said first component by said adsorbent and to depressurize said bed during the desorption steps of said cycle to a desorption pressure so as to desorb said first component from said adsorbent; wherein the ratio of adsorption to desorption pressures ranges from about 1.5 to 3.5,
wherein each bed is configured to be pressurized by pressurized feed gas and with no product pressurization.
11. The system of claim 10 , configured such that the pressure drop across each bed does not exceed about 1.0 psi during desorption and during adsorption.
12. The system of claim 10 , configured such that the pressure drop across each bed does not exceed about 1.5 psi during desorption and during adsorption.
13. The system of claim 10 , wherein each bed is arranged in a radial annular configuration, and said gas mixture exhibits a flow pattern that is transverse to said annular configuration.
14. The system as recited in claim 13 , further comprising: a single stage vacuum pump coupled to each bed for withdrawing an adsorbed component from said bed during a desorption phase of said gas separation method.
15. The system of claim 10 , wherein said gas is air, said first component is nitrogen and said second component is oxygen.
16. The system of claim 15 , wherein the system exhibits a bed size factor <600 lb/TPDO and a specific power consumption <7.5 kW/TPDO.
17. The system of claim 10 , wherein said bed of adsorbent has a dimension, in a direction of flow of said gas through each bed of adsorbent, of less than about 1.2 m and adsorption and desorption steps are performed in a time of less than about 40 seconds.
18. The pressure swing adsorption system of claim 10 which comprises one or more wherein said adsorbent beds are in series or parallel.