Source: http://www.google.de/patents/US8216346
Timestamp: 2013-06-20 01:26:10
Document Index: 776358470

Matched Legal Cases: ['Application No. 61', 'Application No. 61', 'Application No. 61', 'Application No. 09817006', 'Application No. 09816647', 'Application No. 09817000', 'Application No. 09817003']

Patent US8216346 - Method of processing gas phase molecules by gas-liquid contact - Google PatenteSuche Bilder Maps Play YouTube News Gmail Drive Mehr » Erweiterte Patentsuche | Webprotokoll | Anmelden Erweiterte Patentsuche PatenteThe invention relates to a gas liquid contactor and effluent cleaning system and method and more particularly to an array of nozzles configured to produce uniformly spaced flat liquid jets with reduced linear stability. An embodiment of the invention is directed towards a stability unit used with nozzles...http://www.google.de/patents/US8216346?utm_source=gb-gplus-sharePatent US8216346 - Method of processing gas phase molecules by gas-liquid contact Ver�ffentlichungsnummerUS8216346 B2PublikationstypErteilung Anmeldenummer12/950,015 Ver�ffentlichungsdatum10. Juli 2012Eingetragen19. Nov. 2010 Priorit�tsdatum14. Febr. 2005Auch ver�ffentlicht unterUS8088292, US8113491, US8216347, US8262777, US20100089231, US20110061530, US20110061531, US20110072968, US20110081288 Ver�ffentlichungsnummer12950015, 950015, US 8216346 B2, US 8216346B2, US-B2-8216346, US8216346 B2, US8216346B2 ErfinderAndrew R. Awtry, Jason K. Brasseur, Thomas Lee Henshaw, Keith R. Hobbs, David Kurt Neumann, Boris R. NizamovUrspr�nglich Bevollm�chtigterNeumann Systems Group, Inc.Patentzitate (112), Nichtpatentzitate (30), Klassifizierungen (21) Externe Links: USPTO, USPTO-Zuordnung, EspacenetMethod of processing gas phase molecules by gas-liquid contactUS 8216346 B2 Zusammenfassung The invention relates to a gas liquid contactor and effluent cleaning system and method and more particularly to an array of nozzles configured to produce uniformly spaced flat liquid jets with reduced linear stability. An embodiment of the invention is directed towards a stability unit used with nozzles of a gas liquid contactor and/or an enhancer for stable jet formation, and more particularly to reducing the stability of liquid jets formed from nozzles of the gas liquid contactor. Another aspect of the invention relates to operating the apparatus at a condition that reduces the stability of liquid jets, e.g., a droplet generator apparatus. Yet another aspect of the invention relates to operation of the apparatus with an aqueous slurry. Still another aspect of the invention is directed towards to an apparatus for substantially separating at least two fluids.
1. A method of processing gas phase molecules with a gas liquid contactor, comprising the steps of:
forming a plurality of liquid jets from an array of nozzles, wherein a first portion of the plurality of liquid jets comprise a distribution of drops and a second portion of the plurality of liquid jets comprise a substantially flat jet;
providing gas with at least one reactive or soluble gas phase molecule; and
removing at least a portion of the gas phase molecules by a mass transfer interaction between the gas phase molecule and the distribution of drops.
2. The method of claim 1, wherein the distribution of drops comprise droplets having a size in a range from about 50 μm to about 2 mm.
3. The method of claim 1, wherein the distribution of drops comprises a substantially uniform distribution of drops.
4. The method of claim 1, wherein the forming the plurality of liquid jets step comprises operating at plenum pressure in a range from about 13 psi to about 75 psi.
5. The method of claim 1, wherein at least one of the plurality of liquid jets has a velocity greater than 15 m/sec.
6. The method of claim 1, wherein the gas phase molecule comprises at least one of sulfur oxides, nitrogen oxides, carbon dioxide, ammonia, acid gases, amines, halogens, reduced sulfur compounds, and oxygen.
7. The method of claim 1, wherein the gas phase molecule comprises sulfur oxides.
8. The method of claim 1, wherein the gas phase molecule comprises carbon dioxide.
9. The method of claim 1, wherein the gas phase molecule comprises nitrogen oxides.
10. The method of claim 1, wherein the gas phase molecule comprises amines.
11. The method of claim 1, wherein the gas phase molecule comprises chlorine.
12. The method of claim 1, wherein the distribution of drops comprises at least one of water, ammonia, ammonium salts, amines, alkanolamines, alkali salts, alkaline earth salts, peroxides, and hypochlorites.
13. The method of claim 1, further comprising the step of adding an enhancer to decrease the surface tension of the plurality of liquid jets.
14. The method of claim 1, further comprising the step of adding an enhancer to increase a density of the plurality of liquid jets.
15. The method of claim 1, wherein the distribution of drops comprises an aqueous slurry.
16. The method of claim 15, wherein the aqueous slurry comprises a solid material and water in a solution.
17. The method of claim 15, wherein the aqueous slurry comprises solids in a range from about 1 (w/w) to about 20 (w/w).
18. The method of claim 15, wherein the aqueous slurry comprises particles, wherein the particles have particle sizes up to about 500 microns.
19. A method of processing gas phase molecules with a gas liquid contactor, comprising the steps of:
forming a plurality of liquid jets comprising a first substantially stable portion including a plurality of substantially flat jets and a second substantially instable portion including a distribution of drops, wherein the plurality of liquid jets comprises an aqueous slurry comprising solids in a range from about 1 (w/w) to about 20 (w/w);
APPARATUS AND METHOD THEREOF This application claims the benefit of and is a divisional of application Ser. No. 12/586,807, entitled �Gas liquid contactor and effluent cleaning system and method,� filed on Sep. 28, 2009, now U.S. Pat. No. 8,113,491, which is a continuation-in-part of application Ser. No. 12/459,685, entitled �Gas liquid contactor and effluent cleaning system and method,� filed on Jul. 6, 2009, now U.S. Pat. No. 7,866,638, which is a continuation-in-part of application Ser. No. 12/012,568, entitled �Two Phase Reactor,� filed on Feb. 4, 2008, now U.S. Pat. No. 7,871,063, which is a continuation of U.S. patent application Ser. No. 11/057,539, entitled �Two Phase Reactor,� filed on Feb. 14, 2005, now U.S. Pat. No. 7,379,487, and also claims the benefit of U.S. Provisional Application No. 61/100,564, entitled �System for Gaseous Pollutant Removal,� filed on Sep. 26, 2008, U.S. Provisional Application No. 61/100,606, entitled �Liquid-Gas Contactor System and Method,� filed on Sep. 26, 2008, and U.S. Provisional Application No. 61/100,591, entitled �Liquid-Gas Contactor and Effluent Cleaning System and Method,� filed on Sep. 26, 2008; all of which are herein incorporated by reference as if set forth in their entireties.
Φ=φα=k G a(p−p i)=k L a(CL *−C L)
�104 �102 (cm−1)
�102 Packed Column
0.03-2 0.4-2 0.1-3.5
0.5-6 0.5-24
0.1-1 0.07-1.5
Still anther embodiment of the invention is directed towards a method of using an enhancer to reduce instability of jets formed from a nozzle plate of a gas liquid contactor. The method includes applying an enhancer to an inlet stream of a gas liquid contactor to reduce instability of jets formed from the gas liquid contactor. The method also includes forming a plurality of essentially planar liquid jets, each of said liquid jets including a planar sheet of liquid, where the plurality of liquid jets is arranged in substantially parallel planes. Further the method includes providing a gas with at least one reactive or soluble gas phase molecule and removing at least a portion of the gas phase molecules by a mass transfer interaction between the gas phase molecules and the liquid jets.
Each nozzle (520, 522, 524) was formed by cutting a 0.056 inch depth of cut (DOC) into a tube (not shown). The tube was then cut and laser welded into a plate thereby forming the plate of nozzle banks. The tube was stainless steel material having a thickness of 0.90 mm. The nozzle plate was stainless steel material having a thickness of 4.72 mm. Each nozzle is also formed to have a major and minor axis of 2.67 mm and 1.2 mm, respectively. In this Example, nozzle bank 514 and nozzle bank 518 were plugged by filling with a bead of wax, i.e., a high melting point parafin. In addition, in nozzle bank 516, nozzles 520 and 524 were also filled with the same wax material, thereby leaving only one nozzle 522 operational. The plate 512 was then positioned in the apparatus 500 as shown in FIG. 5A. The liquid plenum 509 is arranged above the plate 512 and liquid is configured to flow substantially horizontally across the plate 512. The area ratio between the opening of the nozzle 522 and the liquid plenum is about 1:350.
Example 2 In Example 2, an array of jets was formed with a test stand apparatus as described in Example 1 with a different nozzle plate. FIG. 6A illustrates an entrance side of a nozzle plate including 24 nozzles used in Example 2. Referring to FIG. 6A, the nozzle plate is generally depicted as reference number 600. The nozzle plate 600 includes three nozzle banks 602, 604, and 606. In this configuration each nozzle bank includes twenty four nozzles. Each nozzle is separated by a uniform distance of about 4 mm. The distance between the nozzle banks is also uniform. In this example, the distance between nozzle banks is about 2 cm. In this Example, two of the nozzle banks, 602 and 604, are blocked off with a high melting point parafin wax. The nozzle banks were formed as described in Example 1 and have 0.056 inch DOC.
Fluid/Concentration
Glycol-[100%]
Glycol has a density of 1.1 g/cm3, a viscosity of 16�10−3 kg/m/s, and a surface tension of 48�10−3N/m. Notice the glycol jets are significantly wider than the water jets at the same picture. This is due to the decreased surface tension of glycol compared to water. The density is 1.1 times larger than water, the viscosity is 16 times larger than water, and the surface tension of glycol is 65% of the surface tension of water. The flat jets produced with glycol are noticeably wider than water at the same plenum pressure. This is due to glycol's smaller surface tension compared to that of water.
Run 1-7 psi
Run 2-7 psi
Run 3-9 psi
Run 4-12 psi
Run 5-15 psi
Run 6-17 psi
Run 7-18.5
[ 0.15% by vol.]
Run 4-11
Run 5-9 PSI
Run 1 was used as a control run and compared to Runs 2-5 using Super-water� as an enhancer. Comparing Tables 3 and 4 and FIGS. 9-11, it is shown that less pressure at the liquid plenum is required to form similar sized jets as compared to the previous solution, but with larger surface areas. Also, higher liquid plenum pressures are required for all cases compared to water, however, the formed Super-water� based jets exhibit a higher level of stability. It is also shown that linear sheet instability in the jet depends on the plenum pressure and jet liquid make up. It is important to notice that linear sheet instability is reduced for all Super-water� based solutions.
Each nozzle was formed by cutting a 0.056 inch deep hole into a tube (not shown), i.e., 0.056 DOC nozzle. The tube was then cut and laser welded into a plate thereby forming the plate of nozzle banks. The tube was stainless steel material having a thickness of 0.90 mm. The plate was stainless steel material having a thickness of 6.4 mm. Each nozzle was also formed to have a major and minor axis of 2.67 min and 1.2 mm, respectively.
Example 8 In this Example, an apparatus as shown in FIGS. 13A was utilized with two different jet boxes. The first jet box included nozzles with feed channels only. The second jet box included nozzles with feed channels, a mesh, and a diverter unit with vanes at an angle of about 45 degrees.
Typical reactor operation is near 60 Torr with Cl2/He flowing into the reactor and O2/He flowing out of the reactor, with nominal Cl2→O2 conversion >90%. Standard BHP is m=5 moles/kg KO2H, and has been reacted with Cl2 to <m=1 mole/kg KO2H in our flat jet reactor (Δm=4), with the produced KCl staying in the solution as an insoluble salt. The salt produced in the reaction is the same as the KO2H used, therefore 298 g salt are produced per kg BHP in the Δm=4 reaction. However, there was no noticeable deterioration of the jets during these experiments, even at nearly 30% salt by weight in the slurry.
The tubes of each nozzle were then cut and laser welded into a plate thereby forming the plate of nozzle banks. The tube was stainless steel material having a thickness of 0.90 mm. The nozzle plate was stainless steel material having a thickness of 4.65 mm. In this Example, nozzle bank 514 and nozzle bank 518 were plugged by filling with a bead of wax (high melting point parafin). In addition, in nozzle bank 516, nozzles 520 and 524 were also filled with the same wax material, thereby leaving only one nozzle 522 operational. The plate 512 was then positioned in the apparatus 500 as shown in FIG. 5A. There is also a liquid plenum (not expressly shown) above the plate 512 in which the liquid is configured to flow substantially horizontally across the plate 512. The area ratio between the opening of the nozzle 120 and the liquid plenum is about 1:350.
Na2SO4vs. Gypsum�7 psi:
In this Example, a nozzle plate 600 similar to that shown in FIG. 6A but included four nozzle banks compared to the three nozzle banks shown in the figure was used. The construction of the nozzle plates is similar to that of Example 2. In this configuration each nozzle bank includes twenty four nozzles. Each nozzle is separated by a uniform distance −4 mm. The distance between the nozzle banks is also uniform. In this example, the distance between nozzle banks is 2 cm. For the testing all four of the nozzle banks were run.
Example 13 In Example 13, a test apparatus was utilized to illustrate vacuum stripping of CO2 from an aqueous solution of potassium carbonate (K2CO3), piperazine (PZ) where PZ is 1,4-Diaminocyclohexane) and CO, reaction products which are presumably piperazine carbamate (PZCOO−) and piperazine dicarbamate (PZ(COO−)2) and their protonated forms under normal operating conditions. This Example is applicable to post combustion carbon capture (CO2 capture) systems that require solvent regeneration and CO2 sequestration from a combustion flue gas.
P C ⁢ ⁢ O ⁢ ⁢ 2 reactor = P C ⁢ ⁢ O ⁢ ⁢ 2 cell ⁢ P reactor P cell ⁢ ⁢ P H ⁢ ⁢ 2 ⁢ O reactor = P H ⁢ ⁢ 2 ⁢ O cell ⁢ P reactor P cell Eqs . ⁢ 1 ⁢ - ⁢ 2 FIG. 16 shows a sample spectrum of CO2 stripping data at 60� C. and 23 kPa total pressure according to this Example. The measured partial pressure and flow of CO2 flow desorbing from the flat jet array were 1.93 kPa and 0.61 Standard Liter per Minute, respectively. Once the CO, flow and pressure are measured, the mass transfer coefficient, k, for desorbing from the jets can be calculated using the following equation:
23 kPa CO2 Vapor Pressure (stripper)
0.61 SLM P/P*
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