FIELD OF THE INVENTION

The invention concerns a method and system for regeneration of kinetic hydrate inhibitor (KHI) when it is used without a thenno dynamic hydrate inhibitor (THI).

BACKGROUND OF THE INVENTION

Previously, kinetic hydrate inhibitors have been used together with a thermodynamic inhibitor (normally a glycol, typically monoethylene glycol - MEG). A process for regeneration of both the therm odynamic glycol, and one or more kinetic inhibi tors (while both the thennodynamic and the kinetic inhibitors are in a mixture) has been proposed by ExxonMobil, WO 2006/110192 Al. This patent application describes, in general, a distillation system where water and glycol are separated in a distillation column. Use of thennodynamic inhibitors requires large regeneration units with distillation columns to separate the thermodynamic inhibitor from the aqueous phase. If one adds a KHI to such a loop, the KHI follows the MEG through the system, and there is otherwise no change in the process compared to traditional regeneration processes of THI without KHI, The addition of KHI makes it possible to use lower MEG

concentrations, Otherwise, the ExxonMobil system, is identical to a standard MEG loop. The system is otherwise not changed if a combination of a thermodynamic and a kinetic inhibitor is used, and KHI is subsequently not regenerated from the MEG.

Kinetic inhibitors are used to prevent hydrate formation during transport of

hydrocarbons in presence of water. The kinetic inhibitor is added in low concentrations, typically 0.25-5 wt%. Still, this is an expensive solution and it results in higher discharge of chemicals to the environment, so regeneration of the KHI would be beneficial both for economical and environmental reasons.

SUMMARY OF THE INVENTION

Therefore, it is an object of the invention to provide a method and system for regenerating kinetic hydrate inhibitor which is more economic.

This object is solved with a method and system according to the independent claims. Advantageous further developments are subject of the dependent claims, At present, there is no process for regeneration and reuse of the kinetic inhibitor alone and it is therefore continuously discharged with the produced water.

At present there is a need within the field to effectively prevent hydrate formation during transport of hydrocarbons in the presence of water, while at the same time use less hydrate inhibitor and to do so in a cost effective, energy efficient, compact and environmentally responsible maimer and using less chemicals.

The present invention takes a much different approach and starting point than the prior art. The present invention eliminates the need to use MEG, i.e., transport of the aqueous phase can be conducted without the use of a thermodynamic hydrate inhibitor. This is made possible by the use of kinetic hydrate inhibitor only. This new process is thus not a MEG reclamation process, which also recycles KHI— such as shown in the prior art, rather, a process of recovery of KHI when used without added MEG.

The present invention is related to regeneration of the kinetic inhibitor in systems where it is used without a thermodynamic inhibitor. In addition, this new method and system would require only one evaporation step, whereby the heat required for the evaporation step can be supplied from a heat exchanger. Thus it is not necessary to include a distillation column and this makes the equipment much more compact. The inclusion of heat regeneration from a heat exchanger can thus reduce the energy consumption of the process by more than 90%.

A first aspect of the present invention relates to a method for the regeneration of kinetic hydrate inhibitor used as the sole hydrate inhibitor type, i.e. without the presence of mermodynamic hydrate inhibitor, in a hydrate inhibitor regeneration system, comprising the following steps wherein;

i) a stream containing a mixture of water and kinetic hydrate inhibitor as the sole hydrate inhibitor type, is fed into a flash separator from a feed line;

ii) the water in the flash separator is boiled, i.e. without the use of a distillation column or tower, with heat supplied in an external circulation loop with an external heat exchanger, and escapes as vapor;

iii) kinetic hydrate inhibitor is concentrated in the flash separator and in the circulation loop whereby the kinetic hydrate inhibitor, can be re-used. A second aspect of the present invention relates to the method of the first aspect, wherein heat can be supplied to the flash separator by means of an internal heat exchanger or heating coils located inside the flash separator. A third aspect of the present invention relates to the method of the first or second aspect, wherein the vapor is further heated by compression in a compressor or fan, transferred by means of a vapor conduit and condensed in the external heat exchanger and the heat produced by the condensing vapor is used to heat and evaporate the water in the circulation loop and the separator.

A fourth aspect of the present in venti on relates to a system for the regeneration of kinetic hydrate inhibitor used as the sole hydrate inhibitor type, i.e. without the presence of thermodynamic hytirate inhibitor, wherein, the system is comprised of the following: i) a feed line for feeding water and kinetic hydrate inhibitor into a flash separator; if) an outlet line leading from the flash separator to a pump and a slip stream for withdrawal of regenerated kinetic hydrate inhibitor:

iii) a vapor line for guiding evaporated water vapor from the flash separator, i.e. without the use of a distillation column or tower, to a condenser, and a line connecting a downstream side of the condenser to a condenser drum ;

iv) a return line leading from a heat exchanger to the flash separator.

A fifth aspect of the present invention relates to the system of the fourth aspect, wherein an internal heat exchanger or heating coils are placed inside the flash separator. A sixth aspect of the present invention relates to the system of the fourth or fifth aspect, wherein the vapor line for evaporated water vapor from the flash separator is in. fluid communication with a compressor or fan, followed by a heat exchanger, a condenser drum with two outlets to either a vacuum pump or a pump for warm condensed water, whereby the warm condensed water is in heat exchange contact with inlet streams, and the return line which is located downstream from the heat exchanger and upstream fi-om the flash separator .

A seventh aspect of the present invention relates to the use of the method of the first to third aspect or to a system of the fourth to sixth aspect, for preventing hydrate formation during transport of hydrocarbons in the presence of water. BRIEF DESCRIPTION OF THE FIGURES

Preferred embodiments of the present invention will now be illustrated in more detail with reference to the accompanying figures, in which;

Figure 1 is a principal drawing of the process according to an embodiment of the invention:

Figure 2 is a detailed process description without heat regeneration according to the embodiment shown in Figure 1 ;

Figure 3 is an illustration of a re-boiler with interna! heating according to another embodiment of the invention, and

Figure 4 shows a process of regeneration of kinetic inhibitor with heal regeneration according to another embodiment of the invention.

DETAILED DESCRIPTION OF THE INVENTION

Hydrate is a solid form of water formed at high pressure in presence of light gas molecules normally found in hydrocarbon gases and liquids. Hydrates form a crystalline phase, similar to ice. and may potentially plug flow lines and production equipment. A typical example is the transport of hydrocarbons (gas and/or liquid) in a pipeline in which the temperature drops due to cold surroundings (sea, water or cold air), A water phase may be present at all limes or water may condense as the teraperatai'e drops. At high pressure and low temperature, the water may form hydrates stabilized by the light gas molecules in the hydrocarbon phase.

The traditional method to prevent hydrate formation has been by adding a

thermodynamic hydrate inhibitor. The thermodynamic inhibitor works essentially by diluting the water and thereby reducing the hydrate formation temperature. The amount of inhibitor added depends on the necessary degree of protection, but typically it is 30- 70 wt%. Typical thermodynamic hydrate inhibitors are alcohols such as methanol and ethanol and glycols such as monoethylene glycol (MEG), diethylene glycol (DEG) and triethylene glycol (TEG). Thermodynamic inhibitors are either added batchwise or continuously, in systems with continuous addition of thermodynamic mhibitors, the inhibitor is normally regenerated and reused. This is done in a distillation process where it is separated from water and re-concentrated to a desired concentration. Kinetic hydrate inhibitors are polymer based chemicals that will delay the formation of hydrates, in some cases up to several days. Typical concentration levels are 0.25-5 wt%, but inhibition maybe improved by increasing the concentration. Kinetic inhibitors are not regenerated and are simply discharged with, the produced water. Specific elements in this invention which are new:

Regeneration of kinetic hydrate inhibitor when it is used without a thermodynamic inhibitor can yield the following major improvements: * A distillation column is not necessary which significantly reduces the equipment size.

* Heat integration of the regeneration process leading to very low energy

consumption.

Advantages and improvements achieved by this invention:

At present, kinetic hydrate inhibitors used without a thermodynamic inhibitor are not regenerated. With the present invention, most of the inhibitor may be regenerated and reused. This will:

* Reduce environmental impact because the chemical substance is not discharged with the produced water.

* Allow for use of higher concentration and still reduced cost and environm ental impact.

* Reduce the cost of buying new chemicals. In the present invention, the kinetic inhibitor is regenerated by concentrating it in a re- boiler type unit. A principal drawing is shown in Figure 1. More detailed drawings and explanations of the process are given further below in this description. The produced water stream is fed to a boiler where water is boiled off. The kinetic hydrate inhibitor is a large polymer molecule that has very low vapor pressure. It will not evaporate, but accumulates in the aqueous phase in the re-boiler. Typical examples of kinetic hydrate inhibitor may include poly-(vinyipyrrolidone) (PW), or poly-(vinylcaprolactam) (PVCap) or co-polymers of vinylpyrrolidone or vinylcaprolactam, where the polymer lengths can be variable. Numerous other kinetic hydrate inhibitors are well documented. In the preferred embodiment, the kinetic hydrate inhibitor would have PVP or PVCap functional groups. It is also possible to use mixtures of mentioned compounds depending on operating conditions. When it reaches the desired concentration or the solubility limit, a slip stream is taken out from the re-boiler. The slip stream is concentrated with respect to the irihibitor and is ready for reuse. Due to possible accumulation of impurities, a fraction of the re-concentrated solution may be wasted, Some loss of the kinetic inhibitor should be expected and an addition of some fresh chemical may be necessary. The re-concentrated solution may be pumped back into the pipeline in a separate pipeline or transported in tanks by boat, train or road.

Figure 2 shows a more detailed process description. The aqueous phase containing the kinetic inhibitor is fed to a flash separator 2 through a feed line to one of the alternative locations la, lb or lc. The feed, which is mainly water containing the KHI can have a range of temperature from -5°C to +40 ^C C depending if it comes directly from the pipeline or if there has been some sort of pretreatment, for example separation and/or filtration. It is fed at one of the feed points la _; lb or le. The flash separator 2 is partly liquid filled and the liquid is circulated via an outlet line 3, a circulation pump 4, a line 5, and a heat exchanger 6. The outlet line 3 is exits the flash separator 2 at its bottom section, preferably at the lowermost location of the flash separator 2. Downstream of the outlet line 3, the circulation pump 4 is provided for pumping the circulation stream. The line 5 is provided downstream of the circulation pump 4 in order to connect the circulation pump 4 with the heat exchanger 6, in winch the water is heated before it returns to the flash separator 2 via a return line 7. The way it is added is by circulating the water from the boiler 2 using a pump 4 through a heat exchanger 6 and back in. Typically, the circulation rate will be 10-100 times larger than the feed rate. Heat in the heat exchanger 6 can be supplied, by way of a feed line and return line for heati ng medium (not shown), whereby the hot heating medium is water or oil or steam. When the temperature of the liquid in the flash separator 2 reaches the boiling point, water will escape the flash separator 2 as vapor through a vapor line 8. The amount of heat added by the heat exchanger 6 determines how much water is evaporated which in turn determines the feed rate in the feed line, in. order to keep the liquid level inside the flash separator 2 constant. An altemativ regulation method is to set the rate of feed 1 to a desired rate and adjust the amount of heat supplied in the heat exchanger 6 to regulate the level in the separator 2. If level is increases above the target level, more heat is added and more water will then evaporate to bring the level down. If the level is too low. less heat can be added and less water will evaporate and level will increase. The vapor in the vapor line 8 is fed to a condenser 9 where it is cooled and condensed to water which exits as stream 10 to a condenser drum 11. The stream 10 may contain a gas phase depending on the degree of cooling in the condenser 9 and possible presence of other volatile components and gases. The condensed water is pumped via a line 12 to a pump 13 and is then discharged or sent to further water treatment through a discharge line 14. Noncondensables will leave the condenser drum through a line 15. To reduce the boiling temperature in the system, a vacuum pump 16 could be installed to keep the flash separator at reduced pressure. The discharge from the vacuum pump 16 is sent to an open/closed vent or back into the process.

The kinetic hydrate inhibitor will not evaporate in the flash separator 2 and will therefore accumulate in the circulating liquid exiting the flash separator 2 via outlet line 3. A slip stream 18 may therefore be withdrawn or branched-off from the flash separator 2 downstream of the outlet line 3, preferably in between the circulation pump 4 and the heat exchanger 6, by a regulation valve 19 to produce the regenerated inhibitor stream 20 which can then be reused. Preferably, the regulation valve 19 is provided in a line which is branched-off from line 5.

In Figure 2, the heat for boiling is supplied in an external circulation loop with an external heat exchanger 6 which means that the heat exchanger is provided outside of the vessel of the flash separator 2. The necessary heat may alternatively be added by an internal heat exchanger or heating coils as shown in Figure 3. This is just a

practical/mechanical difference and does not change the composition of any of the product streams or the overall energy consumption.

Figure 4 shows how it is possible to heat integrate the boiler by utilizing the heat from the condensing vapor. The vapor 8 from the flash separator is slightly compressed in a compressor or fan 21. The purpose of compression is to increase the dew point temperature. Compression will also heat the vapor. A vapor conduit 22 guides the hot vapor to the heat exchanger 6 in which the hot vapor is then condensed and this supplies the necessary heat to evaporate the water in the flash separator. The condensed water 23 is collected in the condenser drum 11.

In both cases, the condensed water discharged by the discharge line 14 will be quite hot and can be used in a process-process heat exchanger to heat up the feed stream la-c. Although the foregoing invention has been described in some detail by way of illustration and example for purposes of clarity of understanding, it will be readily apparent to those of ordinary skill in the art in light of the teachings of this invention that certain changes and modifications may be made thereto without departing from the scope of the appended claims.

While the invention has been illustrated and described in detail in the drawings and foregoing description, such illustration and description are to be considered illustrative or exemplary and not restrictive and it is not intended to limit the invention to the disclosed embodiments. The mere fact that certain measures are recited in mutually different dependent claims does not indicate that a combination of these measures cannot be used advantageously. Any reference signs in the claims should not be construed as limiting the scope of the invention.