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A flow conditioning apparatus, a separation system which includes the flow conditioning apparatus and cooperating downstream separation equipment, and a method of using the system are described. The system separates liquid components of differing densities from a fluid mixture. The flow conditioning

A flow conditioning apparatus, a separation system which includes the flow conditioning apparatus and cooperating downstream separation equipment, and a method of using the system are described. The system separates liquid components of differing densities from a fluid mixture. The flow conditioning apparatus includes an inlet, an outlet, and a swirl chamber extending along a swirl axis. The inlet and outlet cooperate with the swirl chamber to create a swirling of a fluid mixture passing through the swirl chamber to ideally induce coalescence of liquid droplets. The inlet and the outlet typically direct fluid to flow in a circumferential direction relative to the swirl axis to create a helical flow. The flow of the fluid mixture through the apparatus encounters a minimum of fluid shear and associated droplet dispersion. The enhanced quantity of droplets coalesced, or at least the quantity of pre-existing droplets entering the control apparatus which are not substantially dispersed by fluid shear, increases the efficiency of liquid separation by the cooperating downstream separation equipment.

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A flow conditioning apparatus, a separation system which includes the flow conditioning apparatus and cooperating downstream separation equipment, and a method of using the system are described. The system separates liquid components of differing densities from a fluid mixture. The flow conditioning

A flow conditioning apparatus, a separation system which includes the flow conditioning apparatus and cooperating downstream separation equipment, and a method of using the system are described. The system separates liquid components of differing densities from a fluid mixture. The flow conditioning apparatus includes an inlet, an outlet, and a swirl chamber extending along a swirl axis. The inlet and outlet cooperate with the swirl chamber to create a swirling of a fluid mixture passing through the swirl chamber to ideally induce coalescence of liquid droplets. The inlet and the outlet typically direct fluid to flow in a circumferential direction relative to the swirl axis to create a helical flow. The flow of the fluid mixture through the apparatus encounters a minimum of fluid shear and associated droplet dispersion. The enhanced quantity of droplets coalesced, or at least the quantity of pre-existing droplets entering the control apparatus which are not substantially dispersed by fluid shear, increases the efficiency of liquid separation by the cooperating downstream separation equipment. roximately 0 to 10.0.3. The method of claim 1 wherein the acid added in step 1 comprises hydrobromic acid.4. The method of claim 1 wherein the acid added in step 1 comprises hydrochloric acid.5. The method of claim 1 wherein the acid added in step 1 comprises an organic acid.6. The method of claim 1 wherein the reducing agent is selected from a group consisting of ammonia, sulfur, hydrogen sulfide, sodium bisulfide, metallic zinc, metallic iron, metallic copper, metallic nickel, metallic cadmium, metallic cobalt, metallic aluminum, metallic manganese, metallic chromium, organic acids, alcohols and aldehydes.7. The method of claim 1 wherein the used fluid comprises an alkali earth metal.8. The method of claim 7 wherein the alkali earth metal is calcium and the alkali used to neutralize excess acid is calcium hydroxide.9. The method of claim 7 wherein the alkali earth metal present in the used fluid is calcium and the alkali used to neutralize excess acid is calcium oxide.10. The method of claim 7 wherein the alkali earth metal present in the used fluid is strontium and the alkali used to neutralize excess acid is strontium hydroxide.11. The method of claim 7 wherein the alkali earth metal present in the used fluid is strontium and the alkali used to neutralize excess acid is strontium oxide.12. The method of claim 1 wherein the alkali used to neutralize excess acid is an alkali metal hydroxide.13. The method of claim 12 wherein the alkali used to neutralize excess acid is sodium hydroxide.14. The method of claim 1 wherein the used halide fluid comprises a base metal and the alkali used to neutralize excess acid is a base metal oxide.15. The method of claim 14 wherein base metal oxide is selected from a group consisting of zinc oxide, copper oxide, cobalt oxide, cadmium oxide and nickel oxide.16. The method of claim 1 wherein the used halide fluid comprises a base metal and the alkali used to neutralize excess acid is a base metal hydroxide.17. The method of claim 16 wherein base metal hydroxide is selected from a group of base metal hydroxides consisting of zinc hydroxide, copper hydroxide, cobalt hydroxide, cadmium hydroxide and nickel hydroxide.18. The method of claim 1 wherein a base metal is used to neutralize excess acid.19. The method of claim 1 wherein the alkali used to neutralize excess acid is ammonia.20. The method of claim 1 wherein steps a-d are performed in a mixed reactor.21. The method of claim 1 wherein separation of the resulting fluid from any suspended solid is performed in a gravity settler.22. The method of claim 1 wherein separation of the resulting fluid from any suspended solid is performed in a clarifer.23. The method of claim 1 wherein separation of the resulting fluid from any suspended solid is performed in a centrifuge.24. The method of claim 1 wherein separation of the resulting fluid from any suspended solid is performed in a pressure filter.25. The method of claim 1 wherein a defoaming agent is used to control excessive foaming in the reaction vessel.26. A method for regeneration of used base metal halide fluids having a density greater than 9.0 lbs./gal. and containing soluble and insoluble impurities, the method comprising: a) adding acid to the used halide so that the pH is within a range of approximately 0 to 5.5; b) contacting the used halide fluid with halogen to increase the density to at least 10.0 lbs./gal., adjust the true crystallization temperature and oxidize impurities; c) adding a reducing agent while maintaining the temperature at a minimum of 10° C.; d) contacting the fluid with an base metal oxide to neutralize excess acid; e) separating any suspended solid impurities from the fluid. 27. The method of claim 26 wherein the reducing agent is selected from a group consisting of anhydrous ammonia, sulfur, hydrogen sulfide, sodium bisulfide, metallic zinc, metallic iron, metallic copper, metallic nickel, metallic cadmium, metallic cobalt, metallic aluminum, metallic