METHOD AND APPARATUS FOR REMOVAL OF OXYGEN FROM SEAWATER

Abstract

Present invention relates to a method for removal of oxygen from seawater comprising the following steps: lead a stream of seawater (1) to be treated and a pressurized stripping gas (2) to a first mixer (3) and mix the seawater (1) with stripping gas (2); lead the combined stream (4) of seawater (1) and stripping gas (2) to a first gas/liquid inline separator (5) and separate the stream (4) into a liquid rich (6) and a gas rich (1 1) phase; lead the liquid stream (6) and a stripping gas stream (7) containing CO2 and water to a second mixer (8) and mix the liquid stream (6) with the gas stream (7); lead the combined stream (9) from the second mixer (8) to a second stage gas/liquid inline separator (10) and separate the combined stream into a liquid rich (14) and a gas rich phase (15); mix the gas stream (1 1) from the first gas/liquid separator (5) with a fresh water stream (22) and lead this combined stream to a first stage scrubber (12) and remove a major portion of the salt entrained in the combined stream from the scrubber (12); lead the salt depleted gas stream (16) from the first scrubber (12) via a heat exchanger or electrical preheater (17) together with a fuel stream (18) to a catalytic deoxidizer (13) and react the fuel (18) and oxygen (19) to a CO2, H20 in the stripping gas stream (7) and mixing this gas stream (7) with the liquid stream (6) from the first stage separator (5); mix the gas stream (15) from the second stage separator (10) with fresh water to remove or dilute the entrained salt in the gas stream (15) and lead the resulting gas stream to a compressor (23); combine the salt depleted gas stream (2) from the compressor (23) and seawater (1) to be treated

Claims

1. A method for removal of oxygen from seawater, the method comprising: leading a stream of seawater to be treated and a pressurized stripping gas to a first mixer and mix the seawater with stripping gas; leading the combined stream of seawater and stripping gas to a first gas/liquid inline separator and separate the stream into a liquid rich and a gas rich phase; leading the liquid stream and a stripping gas stream containing CO.sub.2 and water to a second mixer and mix the liquid stream with the gas stream; leading the combined stream from the second mixer to a second stage gas/liquid inline separator and separate the combined stream into a liquid rich and a gas rich phase; mixing the gas stream from the first gas/liquid separator with a fresh water stream and lead this combined stream to a first stage scrubber and remove a major portion of the salt entrained in the combined stream from the scrubber; leading the salt depleted gas stream from the first scrubber via a heat exchanger or electrical preheater together with a fuel stream to a catalytic deoxidizer and react the fuel and oxygen in the gas stream to form CO.sub.2 and H.sub.2O in the stripping gas stream and mixing this gas stream with the liquid stream from the first stage separator; mixing the gas stream from the second stage separator with fresh water to remove or dilute the entrained salt in the gas stream and lead the resulting gas stream to a compressor; and combining the salt depleted gas stream from the compressor and seawater to be treated.

2. The method according to claim 1, wherein salt amount in seawater entrained in the gas stream from the second separator is removed by mixing the gas stream with fresh water and separate this mixture into a salt depleted gas stream and a liquid stream in a second scrubber.

3. The method according to claim 1, wherein salt entrained in the gas stream from the second stage separator is diluted by injecting fresh water before the gas stream is led to the compressor.

4. The method according to claim 1, wherein the first and second stage separator are in-line separators.

5. The method according to claim 1, wherein the stripping gas is Nitrogen (N.sub.2).

6. The method according to claim 1, wherein the fuel is hydrogen, natural gas, methanol, ethanol or mixtures of any of these.

7. The method according to claim 1, wherein 90-95% of the oxygen in the seawater to be treated is removed in the first stage separator.

8. An apparatus for removal of oxygen from seawater, the apparatus comprising: a first stage mixer for mixing seawater to be treated with a compressed stripping gas; a first stage separator for separating the mixture from the first mixer into a gas stream and a liquid stream; a second stage mixer for mixing the liquid stream from the first stage separator with a gas stream from a subsequent processing step; a second stage separator for separating the stream from the second stage mixer into a gas stream and an oxygen depleted seawater stream; a first stage scrubber for removal of salt entrained in the gas stream from the first stage separator; a heat exchanger or preheater for heating the gas stream from the first stage scrubber; a third mixer for mixing the heated gas stream from the heat exchanger or preheater with a stream of fuel; a catalytic deoxidizer for catalytic deoxidizing of the stream from the mixer; a compressor for compressing the gas stream from the second stage separator; and wherein: the first and second stage separators are in-line separators; the apparatus comprises a second stage scrubber for diluting salt amount in seawater entrained in the gas stream from the second stage separator; and a supply of fresh water is connected to the inlet of the compressor for diluting salt amount in seawater entrained in the gas fed to the compressor.

Description

BRIEF DESCRIPTION OF DRAWINGS

[0041] The invention will be further elaborated in the following description of preferred embodiments with reference to the accompanying drawings, where

[0042] FIG. 1 is a flow sheet showing one embodiment of the system according to the invention.

DETAILED DESCRIPTION OF THE INVENTION

[0043] FIG. 1 shows a preferred embodiment of the system according to the invention. A seawater stream (1) to be deaerated is mixed with a stripping gas stream (2), for example, but not limited to nitrogen, circulated by a compressor or blower (23). This two-phase stream is led through a first stage static mixer (3), providing contact area and turbulent mixing, resulting in oxygen transfer from the liquid to the gas. Typical operating conditions for the static mixer (3) is a pressure of 3-10 barg and a temperature of 0-50 C. The mixed stream (4), containing water, stripping gas, oxygen and salt, is led to a first stage inline separator (5). The first stage inline separator (5) separates gas/water into gas phase (11) and liquid phase (6). Typical operating conditions for the separator (5) is a pressure of 2-10 barg and a temperature of 0-50 C. The gas stream from the inline separator (11) contains stripping gas, oxygen, some water, both vapour and entrained liquid droplets including salt residues. The liquid stream (6) contains water, salt and some oxygen remnants. Typically, 90-95% of the dissolved oxygen in the seawater will be removed in this first stage.

[0044] The gas stream (11) from the first stage in-line separator (5) is mixed with freshwater (22) to dilute salt concentration in the seawater entrained with the gas, before it is passed through a first stage scrubber (12) where the majority of the water and salt residues are removed. Typical operating conditions for this scrubber (12) is a pressure of 2-9 barg and a temperature of 0-50 C. The gas stream (16) is led to a heat exchanger or a pre-heater (17). In one embodiment of the invention, this preheater (17) is an electrical per-heater, while in an alternative embodiment, this pre-heater (17) is a heat exchanger where the cold gas stream is heated by a reaction gas stream from a subsequent deoxidiser (13). A fuel (18) is injected into the heated gas stream (19) before it is led through a static mixer (20), and then to the deoxidiser (13). The fuel can typically be methanol, ethanol, hydrogen or natural gas. The oxygen in the gas stream (19) reacts with the fuel (18) across a catalytic bed in the deoxidiser (13). Product from the chemical reaction (7) is water, and sometimes CO.sub.2 and CO, depending on fuel (18) used. This reaction is exothermic and for this reason, the heat developed through the reaction may be conserved by optionally recycling the hot gas (7) from the deoxidiser (13) through the heat exchanger (17) used for pre-heating the cold stripping gas (16) upstream of the deoxidiser (13). This option is not shown in the drawing. The operating conditions for the deoxidiser are typically a pressure of 2-9 barg and a temperature of 140-550 C.

[0045] The liquid stream (6) from the first stage in-line separator (5) is mixed with the circulating stripping gas stream (7) from the deoxidiser (13). This two-phase stream is led through a second stage static mixer (8) providing contact area and turbulent mixing, resulting in more oxygen transfer from the liquid to the gas. The mixed stream (9) is led to a second stage inline separator (10). This second inline separator (10) separates gas/water into liquid phase (14) of deaerated seawater, and a gas phase (15) containing less oxygen than the gas stream from the first stage (11). Typically will the remaining 5-10% of the initial oxygen be removed in this second stage. The operating conditions for this second in-line separator (10) is a pressure of 1-9 barg and a temperature of 0-50 C. The deaerated seawater (14) from the second in-line separator (10) can be used for injection into gas and/or oil reservoirs.

[0046] The gas stream (15) from the second in-line separator (10) is mixed with fresh water (22) to dilute salt concentration in the seawater entrained with the gas, before it is passed through a second stage scrubber (21) where the majority of the water is removed. The scrubber may be omitted if the compressor/blower (23) can tolerate small amounts of liquid in the gas flow, then fresh water can be injected right upstream of the compressor. The gas stream is circulated by a compressor/blower (23) back to the first stage of the deaeration process, mixing the compressed gas flow (2) with the incoming flow of seawater (1). As the system is pressurized, the outlet water (14) is saturated by a small amount of stripping gas. This loss of stripping gas must be compensated for by use of a top-up gas (24), typically, but not limited to nitrogen or air.