KR20190009848A - Installation for feeding a gas-consuming member with combustible gas and for liquefying said combustible gas - Google Patents

Abstract

The present invention relates to a facility (1) for feeding a combustible gas to a gas consuming member (2, 3, 4) and liquefying the combustible gas, the facility comprising: - sealing and adiabatic tanks (5a, 5b, 5c, 5d) ; - a vapor phase gas collection circuit (6) for withdrawing a combustible gas stream from the tanks (5a, 5b, 5c, 5d); - a heat exchanger (8) comprising a first channel (9) connected to a steam phase gas collection circuit (6); A first channel 9 of the heat exchanger 8 for delivering the combustible gas to the gas consuming members 2 and 3 and 4 and returning the combustible gas to the second channel 10 of the heat exchanger 8; A compressor (11) connected to a three-way connector (12, 13) which can be operated; An expansion device (14) connected to the second channel (10) through a heat exchanger (8) via an intermediate circuit (15); A liquid phase flammable gas stream withdrawn from the tank and a vapor phase combustible gas stream circulating in the steam phase gas collection circuit 6 and a second portion of the combustible gas stream circulating in the intermediate circuit 15, And a cooling device (16) arranged to transfer heat between the cooling device (16).

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention [0001] The present invention relates to a device for feeding a combustible gas to a gas consuming member and liquefying the combustible gas. BACKGROUND OF THE INVENTION 1. Field of the Invention [0001]

The present invention relates to the field of facilities for the treatment of flammable gases such as liquefied natural gas (LNG).

The present invention more particularly relates to a device for feeding a combustible gas to a gas consuming member on the one hand and liquefying the combustible gas on the other hand.

Liquefied natural gas is stored in a liquid / vapor two-phase equilibrium state at a cryogenic temperature in a sealed thermal insulation tank. The insulating barrier of a liquefied natural gas storage tank is the field of heat flow that tends to heat the contents of the tank, which is reflected by the evaporation of liquefied natural gas. Gas derived from natural evaporation is sent to the gas consuming member and used to upgrade it. Thus, for example, in a methane tanker, the vaporized gas is used to feed a power generator to supply the electricity needed for the function of the onboard equipment, or a powertrain to propel the ship. However, although this practice makes it possible to upgrade the gas derived from natural evaporation in the tank, it can not reduce the amount.

Thus, the prior art, in particular US 2015/031 6208, discloses a facility capable of both upgrading a portion of the gas resulting from natural evaporation through one or more gas consuming members and liquefying another part of the gas derived from natural evaporation do. Such a facility includes a collection circuit which draws the vapor phase gas of the gas head space of the tank and then transports it to a heat exchanger for heating within it. Upon exiting the exchanger, the heated gas stream is compressed to a high pressure consistent with the operating conditions of the gas consuming member. The first portion of the compressed gas is then transported to and combusted within the one or more vapor phase gas consuming members while the second portion of the compressed gas is returned to the exchanger and the vapor phase collected in the gas head space of the tank To transfer heat to the gas stream. The second portion of the cooled and partially liquefied gas is then depressurized in the expansion device and in the expansion device it is at least partially re-liquefied by the line-Thomson effect, further reducing the temperature of the gas stream during its expansion . Upon exiting the expansion device, the phase separator returns the liquid phase to the tank and allows the liquid phase and the vapor phase to separate before transferring the gas phase back to the vapor phase gas collection circuit upstream of the heat exchanger.

This arrangement is particularly advantageous in that the compression of the gas stream is used for both making a portion of the gas stream compatible with the operating conditions of the gas consuming member and enabling subsequent re-liquefaction of other portions of the gas stream. Thus, the installation is simplified and the cost of additional re-liquefaction functions is limited.

However, this type of installation is not entirely satisfactory. In particular, under certain critical operating conditions, for example, when the tank is only partially filled, the re-liquefaction yield is low. When the tank is only partially filled, the temperature of the vapor present in the gas head space of the tank is very likely to rise significantly above the equilibrium temperature of the gas. Thus, the exchange of heat between the gas stream collected in the tank and the second part of the compressed gas to be liquefied is insufficient to re-liquefy most of the second part of the compressed gas.

In addition, the gas-phase natural gas derived from natural evaporation is richer in the composition of volatile components, such as nitrogen, than the liquid natural gas in the liquid state stored in the tank. Thus, for liquefied natural gas gasses having a molar concentration of 0.5%, the gas derived from natural evaporation can have a nitrogen concentration of about 14% to 15%. In addition, the use of an expansion device at the outlet of which the steam phase is returned to the vapor phase gas collection circuit while using line-Thomson expansion causes nitrogen to concentrate in the gas stream treated by the installation. Thus, a portion of the compressed gas being conveyed to the one or more gas consuming members may have a nitrogen concentration that is much higher than 20%. Now, a high concentration of nitrogen causes incomplete combustion of the gas in the gas consuming member and results in operating defects in the gas consuming member.

The concept forming the basis of the present invention is to propose a facility for feeding a combustible gas to a gas consuming member which makes it possible to obtain an increased combustible gas liquefaction yield under at least certain critical operating conditions and to liquefy the combustible gas.

According to one embodiment, the present invention provides a facility for feeding a combustible gas to a gas consuming member and for liquefying the combustible gas; These facilities include:

A sealed thermal insulation tank comprising an interior space intended to be filled with flammable gas in a liquid-vapor two-phase equilibrium state;

A vapor phase gas collection circuit comprising an inlet arranged to draw a vapor phase combustible gas stream emerging from the interior space of the tank and from the interior space of the tank; And

A heat exchanger comprising a heat exchange wall for transferring heat from the first and second channels to the first channel, the first channel and the second channel each comprising an inlet and an outlet; The inlet of the first channel being connected to the steam phase gas collection circuit to heat the vapor phase combustible gas stream in a heat exchanger;

A compressor connected upstream of the outlet of the first channel of the heat exchanger to compress the heated combustible gas stream in the heat exchanger and connected downstream to the three-way connector, the three-chamber connector comprising a first portion of the combustible gas stream, The compressor being capable of carrying a second portion of the combustible gas stream to the inlet of the second channel of the heat exchanger to cool the second portion of the combustible gas stream; And

An expansion device connected upstream from the outlet of the second channel of the heat exchanger through the intermediate circuit to the return circuit leading to the tank and connected downstream, the expansion device being arranged to reduce the second portion of the combustible gas stream entering the intermediate circuit ≪ / RTI >

The installation also includes a cooling device including a draw-out circuit, said draw-out circuit comprising an inlet arranged to draw a liquid phase flammable gas stream of the internal space of the tank as it appears in the internal space of the tank; The cooling device includes a liquid phase flammable gas stream withdrawn from the tank and a steam phase combustible gas stream circulating in the steam phase gas collection circuit and a heat To cool the flammable gas stream to be cooled using a latent heat of vaporization of the liquid phase flammable gas stream withdrawn from the tank and withdrawn from the tank.

The present invention therefore proposes to use the liquid phase of the combustible gas stored in the tank to further reduce the temperature of the compressed gas at the inlet of the expansion device, Or by reducing the temperature of the gas at the inlet of the first channel of the heat exchanger such that the temperature at the outlet of the second channel of the exchanger is consequently reduced . Thus, by reducing the temperature of the gas stream at the inlet of the expansion device, the degree of liquefaction thereof during its decompression in the expansion device is substantially increased. This makes it possible to obtain an increased liquefaction yield under certain critical operating conditions, especially when the temperature of the vapor present in the gas head space of the tank significantly exceeds the equilibrium temperature of the gas.

Additionally, when the combustible gas is a gas mixture of the LNG or LPG type containing nitrogen in a small proportion and when the cooling device is arranged to carry the vaporized gas stream in the vapor phase gas collection circuit, Enables the dilution of the nitrogen of the intended gas stream to be carried out, allowing the re-liquefaction yield to be adjusted to the operating conditions of the gas consuming member without substantially degrading it.

According to embodiments, such a facility may include one or more of the following features.

According to one embodiment, the combustible gas is a gas mixture of the LNG or LPG type comprising nitrogen.

According to one embodiment, the combustible gas is a gas mixture comprising nitrogen and the nitrogen is the highest volatile component of the gas mixture.

According to one embodiment, the cooling device is arranged to return the vaporized gas stream of the cooling device to the vapor phase gas collection circuit to reduce the nitrogen content of the combustible gas stream circulating in the vapor phase gas collection circuit.

Thus, when the combustible gas is composed of a gaseous mixture comprising nitrogen, this is because the vaporized gas stream of the cooling device flows from a gas stream withdrawn from the liquid phase from a tank having a reduced concentration of the highest volatile compound such as nitrogen To reduce the nitrogen concentration in the vapor phase being treated. This, in turn, makes it possible to keep the nitrogen concentration of the gas being treated by the installation within a range that can coexist with the exact function of the gas consuming member. In addition, the liquefaction yield will be greater as the vapor phase gas at the facility entrance has less volatile component-rich composition. As a result, by mixing the gas stream entering from the natural evaporation with the vaporized gas stream of the cooling device, the nitrogen concentration of the resulting mixture is reduced, which makes it possible to increase the liquefaction level during decompression in the expansion device.

According to a first embodiment the cooling device comprises an additional heat exchanger and the additional heat exchanger includes a heat exchange wall for transferring heat from the first and second channels and the first channel to the second channel of the additional heat exchanger Wherein the first channel and the second channel each include an inlet and an outlet, the first channel is integrated into an intermediate circuit connecting the heat exchanger and the expansion device, the inlet of the second channel is connected to the inlet of the cooling device, The outlet of the second channel is connected to a vapor phase gas collection circuit.

According to a variant of the first embodiment, the additional heat exchanger is superimposed on the heat exchanger and the outlet of the second channel of the additional heat exchanger is connected to the inlet of the first channel of the heat exchanger such that the liquid phase gas stream is supplied to the additional heat exchanger Can be flowed by gravity from the outlet of the two channels to the inlet of the first channel of the heat exchanger.

According to a second embodiment variant, the cooling device comprises a second additional channel comprising a first channel incorporated in the vapor phase gas collection circuit and a second channel comprising an inlet connected to the outlet phase circuit and an outlet connected to the vapor phase gas collection circuit, And a heat exchanger.

According to a second embodiment, the cooling device comprises a chamber and a spray element integrated in the vapor phase gas collection circuit between the inlet of the steam phase gas collection circuit and the inlet of the first channel of the heat exchanger, And is arranged to spray a liquid phase combustible gas into the chamber to cool the vapor phase gas stream withdrawn from the interior space of the tank and reduce the nitrogen content of the combustible gas stream circulating in the vapor phase gas collection circuit.

According to a variant of any of the three preceding embodiments, the cooling device includes a pumping device that sucks the liquid phase flammable gas stream through the inlet of the cooling device and delivers it to the withdrawal circuit.

According to one embodiment, the installation includes a gas analyzer capable of delivering a representative measurement of the nitrogen concentration of the first portion of the combustible gas stream, wherein the control unit is configured to monitor the first portion of the combustible gas stream Is arranged to produce a control signal of the pumping device as a function of a representative measurement of the nitrogen concentration of the first portion of the combustible gas stream delivered to the gas consuming member to assure a nitrogen concentration.

According to one embodiment, the gas analyzer can analyze the composition of the gas sample to derive its nitrogen concentration therefrom. According to another embodiment, the gas analyzer is a machine for measuring the upper heating power of a gas sample.

According to one embodiment variant, the control unit controls the concentration of nitrogen in the first portion of the combustible gas stream as a function of a representative measurement of the nitrogen concentration of the first portion of the combustible gas stream and a nominal concentration below the limiting operating concentration of the gas consuming member And to generate a control signal for the pumping device to subordinate to the nominal concentration.

According to another alternative embodiment, the control unit

Control of the pumping device to subordinate the nitrogen concentration of the first portion of the combustible gas stream to the nominal concentration as a function of a representative measurement of the nitrogen concentration of the first portion of the combustible gas stream and a nominal concentration less than the limiting operating concentration of the gas consuming member A nitrogen concentration preference mode arranged to generate a signal; And

- generating a control signal for the pumping device to arrange the temperature (T1) for the nominal temperature as a function of the nominal temperature and a temperature measurement (T1) of the second part of the gas stream circulating in the intermediate circuit of the inlet of the expansion device A re-liquefaction priority mode;

The control unit is arranged to switch from a nitrogen concentration preference mode to a re-liquefaction preference mode as a function of a representative measurement of the nitrogen concentration of the first portion of the combustible gas stream.

According to one embodiment, the cooling device comprises a sensor and a control unit capable of measuring the temperature (T1) of the second part of the gas stream circulating in the intermediate circuit of the inlet of the expansion device, To produce a control signal for the pumping device to subordinate the temperature (T1) to the nominal temperature as a function of the temperature of the temperature (T1) and the nominal temperature.

According to a first variant, the pumping device comprises a pump, and the control unit is arranged to steer the pump as a function of the control signal. In other words, the liquid phase gas flow delivered by the pump of the pumping device is varied to obtain the desired flow rate.

According to a second variant, the pumping device comprises a pump and a return pipeline, wherein the return pipeline is connected to the draw-out circuit downstream of the pump, firstly to the internal space of the tank and to the two valves, Valves are respectively installed in the withdrawing circuit downstream of the return pipeline connector and in the return pipeline; The control unit is arranged to steer one and / or the other of the two valves as a function of the control signal. In other words, the pump of the pumping device operates at a constant power, one of the two valves and the remainder of the liquid phase gas stream returned to the tank through the return pipeline and the portion of the liquid phase gas stream And is operated to modify the distribution between the parts.

According to one embodiment, the expansion device is an expansion valve, also known as a Joule-Thomson valve.

According to one embodiment, the installation comprises a phase separator connected to the return device leading from the upstream to the expansion device and from the downstream to the tank to the return, and on the other hand to the return pipe connected to the steam phase gas collection circuit; The phase separator is arranged to carry the liquid phase of the combustible gas stream to the return circuit and convey the gas phase of the combustible gas stream to the return pipe.

According to an advantageous variant, the compressor is a multi-stage compressor. Advantageously, the compressor comprises a plurality of compression stages and a plurality of intermediate heat exchangers, each intermediate heat exchanger being disposed at one of the compression stages.

According to one embodiment, the present invention also provides a method for dispensing a combustible gas to a gas consuming member and liquefying the combustible gas by the above-described apparatus; This way:

Conveying the vapor phase combustible gas stream from the inlet of the steam phase gas collection circuit to the inlet of the first channel of the heat exchanger;

Transferring heat from the second channel to the first channel of the heat exchanger;

Compressing the combustible gas stream exiting the first channel of the heat exchanger;

Conveying the first portion of the compressed combustible gas stream to the gas consuming member and returning the second portion of the compressed gas stream to the inlet of the second channel of the heat exchanger;

Conveying a second portion of the combustible gas stream from the second channel of the heat exchanger through the intermediate circuit to the expansion device;

- depressurizing a second portion of the combustible gas stream entering from the intermediate circuit;

Conveying at least one liquid phase portion of the second portion of the reduced pressure combustible gas stream to the tank;

Withdrawing a liquid phase flammable gas stream from the interior space of the tank;

Transferring heat between the liquid phase flammable gas stream withdrawn from the tank and the steam phase gas stream circulating in the steam phase gas collection circuit and the cooled gas stream selected from the second portion of the gas stream circulating in the intermediate circuit, Vaporizing the drawn liquid phase combustible gas stream and using a latent heat of vaporization of the liquid phase combustible gas stream withdrawn from the tank to cool the gas stream to be cooled.

According to one embodiment, the combustible gas is a gas mixture comprising nitrogen and the vaporized gas stream in the cooling device is returned to the vapor phase gas collection circuit.

According to one embodiment, a variable indicative of the nitrogen concentration of the first portion of the combustible gas stream is measured and the flow rate of the liquid phase combustible gas stream circulating in the withdrawal circuit of the cooling device is determined by the nitrogen concentration of the first portion of the combustible gas stream Is adjusted as a function of the variable indicating.

According to an alternate embodiment, the flow rate of the liquid phase combustible gas stream circulating in the withdrawal circuit of the refrigeration device is determined by the concentration of the first portion of the combustible gas stream as a function of the nominal concentration and the variable representing the nitrogen concentration of the first portion of the combustible gas stream The nitrogen concentration is adjusted to subordinate to the nominal concentration.

According to one embodiment, in at least one operating mode, the temperature (T1) of a second portion of the gas stream circulating in the intermediate circuit upstream of the expansion device is measured and the liquid phase flammable gas The flow rate of the stream is adjusted as a function of the nominal temperature and the measurement of the temperature (T1) so as to subordinate the temperature (T1) to the nominal temperature.

According to an advantageous variant, the combustible gas is liquefied natural gas and the nominal temperature (T1) is between -145 and -160 ° C.

According to one embodiment, the present invention provides a vessel comprising the above-described facility.

According to one embodiment, the present invention also provides a method of loading or emptying a flammable gas into such a vessel through which the flammable gas is delivered via a cryogenic transfer pipe from a floating or land based storage facility to a tank of a vessel or vice versa.

According to one embodiment, the present invention also provides a system for delivering flammable gas, the system comprising a vessel as described above, a cryogenic transfer pipe arranged to connect a tank installed in the hull of the vessel to a floating or land based storage facility, And a pump for driving the combustible gas stream through the cryogenic transfer pipe from a floating or land-based storage facility to the vessel's tank or vice versa.

BRIEF DESCRIPTION OF THE DRAWINGS The present invention will now be better understood from the following description of some specific embodiments of the invention given by way of illustration only and not by way of limitation with reference to the accompanying drawings, It will be clearer.
1 is a schematic view of a facility for feeding a combustible gas to a gas consuming member according to the first embodiment and for liquefying the combustible gas;
2 is a schematic view of a facility according to a second embodiment;
3 is a schematic view of a facility according to a third embodiment;
Figure 4 illustrates an arrangement of two heat exchangers of Figure 2 in a detailed manner in accordance with an embodiment variant.
5 shows an example of the nitrogen concentration of the different natural gas streams of the plant of FIG. 2 as a function of the nitrogen concentration of the liquid natural gas when 70% of the flow of the combustible gas stream returns to the heat exchanger and is re- Respectively.
6 is a graph similar to that of FIG. 5 when 70% of the flow of the combustible gas stream returns to the heat exchanger and is re-liquefied therein.
Figure 7 shows the flow rate of the liquid phase gas drawn from the tank as a function of the flow rate of the second part of the combustible gas stream returning to the inlet of the second channel of the heat exchanger for the installation of Figure 1 and the arrangement of Figure 2, Which is a graph showing the difference between the flow rates of the gases.
Figure 8 is a schematic view of the first part of the gas stream being conveyed to the gas consuming member as a function of the flow rate of the second part of the combustible gas stream returning to the heat exchanger for the installation according to figure 1 or 2 and for the arrangement according to the prior art Nitrogen concentration.
- Figure 9 shows the flow rate of the liquid phase gas drawn out of the tank as a function of the flow rate of the second part of the combustible gas stream returned to the heat exchanger for the plant according to Figure 2 and the prior art equipment, In the graph of FIG.
10 is a schematic view of a ship and a delivery system for loading / unloading a combustible gas;

In the specification and claims, the term "combustible gas" has a generic character and refers to a gas mixture consisting of a single pure material or a plurality of components without distinguishing.

In Fig. 1, there is illustrated a facility 1 for feeding a combustible gas to one or more gas consuming members, on the one hand, and liquefying a combustible gas, on the other hand. Such a facility 1 may be installed on a land or floating structure. In the case of a floating structure, the installation 1 may be for a liquefied natural gas cargo ship such as a methane tanker or for a liquefied or regasified barge, or more generally for any vessel with a gas consuming element

The plant 1 comprises three different types of combustible gas consuming elements, namely a burner 2, a generator 3 and an engine 4 for propelling the ship.

The burner 2 may be integrated into a power production facility or integrated into a gas combustion unit (GCU). The power production facility may in particular include a steam generating boiler. The steam may be for feeding to the steam turbine for energy production and / or for feeding the ship to the heating network. The burner 2 can function as a flammable gas whose nitrogen concentration is high, for example 30% to 35% larger than the standard gas combustion unit, but which can far exceed this by supplying fuel .

The generator 3 includes, for example, a diesel / natural gas mixed feed heat engine of DFDE (dual-fuel diesel) technology. Such a heat engine can burn a mixture of diesel and natural gas or use one or the other of these two fuels. The natural gas supplied to such a heat engine must have a pressure on the order of a few bar to several tens of bar, for example about 6 to 8 bar (absolute pressure). In addition, in order to allow functions compatible with this heat engine, the natural gas must have a nitrogen concentration below the limiting operating concentration of about 15% to 20%.

The engine 4 for propelling the boat is, for example, a dual fuel two-stroke low-speed engine of the "ME-GI" technology developed by MAN. This engine 4 uses natural gas as a combustible material and a small amount of pilot fuel injected before natural gas injection to ignite the natural gas. In order to feed these engines 4, the natural gas must first be compressed at high pressures between 150 and 400 bar (absolute pressure), in particular between 250 and 300 bar (absolute pressure). In addition, such engines are highly sensitive to the quality of natural gas, and to enable adaptive function, the natural gas must have a nitrogen concentration that does not exceed a threshold value of 15% to 20%.

The installation 1 comprises at least one enclosed and adiabatic tank 5a, 5b, 5c, 5d. According to one embodiment, each tank 5a, 5b, 5c, 5d is a membrane tank. By way of example, such membrane tanks are described in patent applications WO 14/057221, FR 2 691 520 and FR 2 877 638. Such membrane tanks are intended to store flammable gases at substantially the same or slightly higher pressure than the atmospheric pressure. According to another alternative embodiment, each tank 5a, 5b, 5c, 5d may also be a self-contained tank, and in particular may have a parallelepiped, prismatic, spherical, cylindrical or multi-leaf configuration. Certain types of tanks 5a, 5b, 5c, 5d permit gas storage at pressures substantially higher than atmospheric.

Each tank 5a, 5b, 5c, 5d includes an interior space intended to be filled with a combustible gas. The flammable gases are in particular liquefied natural gas (LNG), which is mainly methane and also one or more other hydrocarbons such as ethane, propane, n-butane, i-butane, n-pentane, i-pentane, neopentane, ≪ / RTI > The flammable gas may also be a mixture of ethane or liquefied petroleum gas (LPG), i.e., hydrocarbons derived from propane and butane and essential oils essentially containing a small percentage of nitrogen.

The combustible gas is stored in the internal space of each tank 5a, 5b, 5c, 5d in a liquid-vapor two-phase equilibrium state. Thus, the gas is present in the vapor phase of the upper part of the tanks 5a, 5b, 5c, 5d and in the liquid phase of the lower part of the tanks 5a, 5b, 5c, 5d. The equilibrium temperature of the liquefied natural gas corresponding to the liquid-vapor two-phase equilibrium state is about -162 ° C when stored at atmospheric pressure.

The facility 1 includes a vapor phase gas collection circuit 6 which includes an inlet 7a, 7b, and 7c that appears above the maximum charge height of the tank, i.e., the gas head space of each tank 5a, 5b, 5c, 7c and 7d. These inlet portions 7a, 7b, 7c and 7d are connected to the vapor phase gas collection circuit 6 via a valve 24.

The steam phase gas collection circuit 6 leads to a heat exchanger 8. The heat exchanger 8 has a first and a second heat exchanger 12 having heat exchanging walls for transferring heat from the inlets 9a and 10a and the outlets 9b and 10b to the first channel 9 from the second channel 10, Channels 9,10. To optimize heat exchange, the heat exchanger 8 is a countercurrent exchanger. The inlet 9a on the first channel 9 is connected to the vapor phase gas collection circuit 6 for heating the gas stream derived from the natural evaporation collected in the tanks 5a, 5b, 5c, 5d. The outlet 9b of the first channel 9 is connected to a compressor 11 for compressing the gas stream at a pressure compatible with the operation of the gas consuming member.

In the illustrated embodiment, the compressor 11 is a multi-stage compressor. In other words, the compressor 11 is provided with a plurality of compression stages 11a, 11b, 11c, 11d and 11e and intermediate heat exchangers 33a and 33b arranged at the outlets of the respective compression stages 11a, 11b, 11c, , 33c, and 33d. The intermediate heat exchangers 33a, 33b, 33c and 33d are for cooling the compressed gas between the two compression stages 11a, 11b, 11c, 11d and 11e. For example, the heat exchangers 33a, 33b, 33c, 33d may provide an exchange with, inter alia, seawater so that the compressed gas stream may be at a temperature substantially equal to the temperature of the seawater.

The compressor 27 is dimensioned as a function of the combustible gas consuming member to be fed, in particular as a function of the pressure level at which the combustible gas is to be fed and its maximum feed rate. Thus, when one of the gas consuming members is an ME-GI type engine 4 as described above, the compressor 11 will typically have a gas stream leaving the compressor 11 between 250 and 300 bar (absolute pressure) Dimensions are set to have pressure.

Downstream of the compressor 11 the installation 1 delivers a first portion of the gas stream to the engine 4 and a second portion of the gas stream to the second channel 10 of the heat exchanger 8 And a three-way connector 12 for carrying it to the inlet 10a. The three-way connector 12 is steered by the control unit 34. The control unit 34 therefore controls the inlet 10a and the engine 4 of the second channel 10 of the heat exchanger 8 as a function of the combustible gas demand of the engine 4 and / The ratio of the gas circulating in each case can be changed.

In addition, in the case where the combustible gas consuming member has different feed pressures as in the illustrated embodiment, the installation 1 includes an intermediate three-chamber connector 13 disposed between the two compression stages 11b and 11c , Thus making it possible to divert a portion of the gas stream to the gas consuming member, in this case the burner 2 and the generator 3, before the outlet of the compressor 11. This arrangement makes it possible to pass the combustible gas through a sufficient number of compression stages (11a, 11b) and then to direct the combustible gas to the combustible gas consuming member so as to reach the delivery pressure corresponding to the consumable member.

The second portion of the combustible gas stream is cooled while the heat is transferred from the second channel 10 of the heat exchanger 8 to the vapor phase gas exiting the vapor phase gas collection circuit 6.

The outlet 10b of the second channel 10 of the heat exchanger 8 is connected to the outlet of the second channel 10 at a pressure substantially equal to the pressure present in, for example, the tanks 5a, 5b, 5c and 5d, Is connected to the phase separator 25 through an expansion device 14 which is depressurized to a near pressure. As a result, the gas stream undergoes an expansion that at least partially leads to a reduction in its temperature and its liquefaction through the joule-Thomson effect. The expansion device 14 is, for example, an expansion valve.

A phase separator 25, also referred to as a mist separator, allows the liquid phase to separate from the gas phase. Downstream, the phase separator 25 is connected to the return circuit 31 leading to the tanks 5a, 5b, 5c and 5d on the one hand and to the return pipe 31 connected to the steam phase gas withdrawing circuit 6 32. The phase separator 25 therefore conveys the liquid phase of the combustible gas to the tanks 5a, 5b, 5c and 5d while the vapor phase is connected to the inlet 9a of the first channel 9 of the heat exchanger 8 Is returned.

The plant 1 also includes a cooling device 16 for cooling the steam phase gas stream circulating in the steam phase gas collection circuit 6. [ To this end, the cooling device 16 comprises a chamber 20, which is integrated in a vapor phase gas collection circuit 6 and a liquid phase flammable gas stream drawn from one of the tanks 5c is sprayed therein . Thus, the atomized combustible gas stream is vaporized, depriving it of the steam phase gas stream collected in the gas head space of the tank. In addition, atomization and vaporization of a portion of the liquid phase flammable gas can at least partially reduce the concentration of the highest volatile component, especially nitrogen, in the gas stream intended to be delivered to the gas consuming member 2, 3, 4.

The cooling device 16 includes a draw-out circuit 35. The withdrawing circuit 35 has an inlet 27 which is connected to the tank 5a, 5b, 5c at the bottom of the tank, proximate to the base of the tank to draw out the liquid phase of the flammable gas stored in the tank, 5c, < RTI ID = 0.0 > 5d. ≪ / RTI > The cooling device 16 also sucks the liquid phase flammable gas through the inlet 27 of the cooling device 16 and delivers it to the at least one spray element 21 in the chamber 20 And a pumping device capable of circulating.

In the illustrated embodiment, the pumping device comprises:

A pump 26 for sucking and delivering the liquid phase flammable gas stream;

A return pipeline 37 connected on the one hand to the draw-out circuit 35 downstream of the pump 26 and on the other hand in the internal space of the tank 5c; And

- two valves 38, 39, respectively, provided on the withdrawing circuit 35 downstream of the connection of the return pipeline 37 to the withdrawing circuit 35 and on the return pipeline 37, do.

The cooling device 16 also includes a control unit 36 for controlling the pumping device. The control unit 36 is connected to the temperature sensor 29 and the gas analyzer 40. The sensor 29 is arranged in the intermediate circuit 15 and thus can deliver a temperature measurement T1 of the second part of the compressed gas stream circulating in the intermediate circuit 15 at the inlet of the expansion device 24 . The gas analyzer 40 can deliver a measurement indicative of the nitrogen concentration of the gas stream intended to be delivered to the gas consuming member 2, 3, 4.

According to one embodiment, the gas analyzer 40 can analyze the composition of the sample of the gas stream and thus determine the nitrogen concentration of the gas stream intended to be delivered to the gas consuming member. 1, the gas analyzer 40 preferably draws a sample of the gas between the compressor 11 and the outlet 9b of the second channel 9 of the heat exchanger 8. In this case, . Thus, the analyzed gas sample is primarily preheated and, secondly, at atmospheric pressure or at substantially atmospheric pressure, which facilitates analytical operation. The gas analyzer 40 may however be positioned differently.

According to another embodiment, the gas analyzer 40 is a machine for measuring the upper heating power of the combustible gas. The upper heating power is a characteristic of the nitrogen concentration, and the heating power is a representative measure of the nitrogen concentration of the gas stream. In this case, the gas analyzer 40 is advantageously incorporated into one or more gas consuming members 2, 3, 4.

The control unit 34 is able to determine the limit operating concentration for the gas consuming member (s) 2, 3 and 4, that is, the correct function of the gas consuming member (s) (2), (3), (4) that are below the limit nitrogen concentration that does not exceed the limit nitrogen concentration.

According to a first prediction approach, the amount of liquid phase combustible gas stream delivered by pump 26 is determined by a digital modeling tool. The digital modeling tool makes it possible to determine the flow rate of the nominal liquid phase flammable gas stream delivered by the pump 26, which on the one hand is a gas which is below the limit operating concentration of the gas consuming member (s) 2, 3, 4 Enables the nitrogen concentration of the gas stream intended to be delivered to the consuming member (s) (2, 3, 4) to be guaranteed, and on the other hand enables optimization of the degree of re-liquefaction during Row-Thomson decompression.

The modeling tool in particular determines the flow rate of the nominal liquid phase flammable gas stream drawn as a function of the following inlet parameters:

- the respective nitrogen concentration of the gas phase and / or liquid phase of the gas stream intended to be delivered to the gas consuming member (s) (2, 3, 4) and / or of the combustible gas stored in the tank;

A steam phase gas stream flow circulating in the steam phase gas collection circuit (6); And

The ratio between the first portion of the compressed combustible gas stream delivered to the gas consuming member (s) (2, 3, 4) and the second portion of the compressed combustible gas stream returned to the exchanger (8).

If the nitrogen concentration of the gas stream intended to be delivered to the gas consuming member (s) 2, 3, 4 is less than the critical threshold, the control unit 36 operates in the re-liquefied priority mode, The flow rate of the liquid phase combustible gas stream is determined such that the temperature (T1) of the second portion of the gas stream circulating in the intermediate circuit 15 is subordinate to the nominal temperature. Thus, in this redistribution preference mode, the flow rate of the combustible gas stream is determined to optimize the degree of re-liquefaction. When the combustible gas is a liquefied natural gas stored at atmospheric pressure, the nominal temperature for the second part of the gas stream circulating in the intermediate circuit 15 is typically between -145 캜 and -162 캜, for example around -160 캜 .

In contrast, when the nitrogen concentration of the gas stream intended to be delivered to the gas consuming member (s) 2, 3, 4 is equal to or greater than the critical threshold, the control unit 36 operates in the nitrogen concentration preference mode , In a nitrogen concentration preference mode, it is determined that a representative measure of the nitrogen concentration of the gas stream intended to be delivered to the gas consuming member (s) is the flow rate of the withdrawn liquid phase combustible gas stream is subordinate to the target concentration. The target nitrogen concentration may exceed the limit concentration of the gas consuming member (s) to be fed, for example, less than 2% of the limit concentration of the gas consuming member (s) to be fed, where the correct function of the gas consuming member (s) To about 3%.

According to a second approach, the flow rate of the liquid phase flammable gas stream delivered by the pump 26 is controlled such that the representative measurement of the nitrogen concentration of the gas stream circulating in the vapor phase gas collection circuit 6, for example, Or by adjustment of the PID type. The target nitrogen concentration of the gas stream circulating in the vapor phase gas collection circuit is determined as a function of the limiting concentration of the gas consuming member (s) (2, 3, 4) supplied.

According to one embodiment, it is possible to combine the first and second approaches described above.

The increase in consumption of the gas consuming member (s) 2, 3, 4 also reduces the occurrence of a momentary increase in nitrogen concentration in the gas stream at the inlet 9a of the first channel 9 of the heat exchanger 8 It is easy to provide. Specifically, during the increase of the flow rate of the first portion of the combustible gas stream delivered to the gas consuming member (2, 3, 4) relative to the flow rate of the second portion of the stream returned to the exchanger 8, A transient phenomenon has been observed which promotes the gas stream circulating in the intermediate circuit 32 at the inlet 9a of the first channel 9 of the exchanger 8 for the gas stream entering from the space, Resulting in a transient increase in the nitrogen concentration of the gas stream at the inlet 9a of the first channel 9 of the first channel 9, Thus, according to one embodiment, to compensate for this phenomenon, the control unit 33 can determine whether the drift of the flow rate of the first portion of the gas stream carried to the gas consuming member (s) 2, 3, 4 is positive And has a calibration factor to increase the nominal flow rate.

According to the first embodiment, the pump 26 operates at a constant power to provide a constant flow rate and the control unit 36 has two valves 38, 38 as a function of the nominal flow rate determined by the control unit 33, 39, < / RTI > Thus, the delivery rate of the pump 26 is constant and one of the two valves 38, 39 and / or the remainder is part of the liquid phase flammable gas stream being transported to the spraying member (s) Lt; RTI ID = 0.0 > a < / RTI >

According to the second embodiment, the valve 38 is closed while the valve 39 is open and the control unit 36 generates a signal for controlling the pump 26 to change its delivery rate.

According to an embodiment variant not shown, the installation 1 comprises an additional phase separator at the outlet of the chamber 20. This phase separator is intended to guide the undigested liquid phase in the chamber 20 to the return circuit 31 which is primarily followed by the tanks 5a, 5b, 5c and 5d and, secondly, (9a) of the first channel (9) of the channel (8).

With reference to Fig. 2, a facility 1 according to a second preferred embodiment is shown. Which differs from the previous facility described only for the characteristics of the cooling device 16.

2, the cooling device 16 includes an additional heat exchanger 17 that ensures the transfer of heat without exchange of material between the compressed gas stream circulating in the intermediate circuit 15 and the liquid phase gas stream collected in the tank do.

To this end, the additional heat exchanger 17 includes first and second channels 18, 19, which include inlets 18a, 19a and outlets 18b, 19b, respectively. To optimize heat exchange, the additional heat exchanger 17 is advantageously a countercurrent exchanger. The first channel 18 is incorporated in the intermediate circuit 15 connecting the heat exchanger 8 and the expansion device 14. [ In other words, the inlet 18a of the first channel 18 is connected to the outlet 10b of the second channel 10 of the heat exchanger 8 and the outlet 18b of the first channel 18 is connected to the outlet (14). The inlet 19a of the second channel 19 is connected to the extraction circuit 35 while the outlet 19b thereof is connected to the vapor phase gas extraction circuit 6. [

In other words, the embodiment of Figure 2 is particularly advantageous in the following respects:

Firstly, heat is drawn from the second part of the compressed gas stream circulating in the intermediate circuit 15, which is particularly advantageous with respect to the liquefaction performance;

Secondly, the vaporized gas stream is injected into the gas stream circulating in the vapor phase gas collection circuit 6, which is the nitrogen of the gas stream intended to be delivered to the gas consuming member (s) 2, 3, 4 Is particularly advantageous with regard to reducing the concentration.

The pumping device shown in Figure 2 is simpler than that described with respect to Figure 1 because it includes only one pump 26. [ The apparatus 1 also includes a gas analyzer 40 and an additional heat exchanger 17 for delivering representative measurements of the nitrogen concentration of the gas stream intended to be delivered to the gas consuming member (s) 2, 3, And a sensor 28 for measuring the temperature T1 of the second portion of the gas stream at the outlet 18b of the first channel 18, i.e. at the inlet of the expansion device 14. [ As in the embodiment of Figure 1, the control unit 36 is designed to communicate with the gas consuming member (s) 2, 3, 4 which are below the threshold operating concentration of the gas consuming member (s) 2, 3, To produce a signal for controlling the pump 26 to ensure the nitrogen concentration of the gaseous stream.

Under certain operating conditions, particularly when the nitrogen concentration of the gas stream intended to be delivered to the gas consuming member (s) 2, 3, 4 is high, it is withdrawn from the tanks 5a, 5b, 5c, The liquid phase gas flow intended to be injected into the vapor phase gas collection circuit 6 can be found to be too high to be fully vaporized in the additional heat exchanger 17. In other words, the gas stream at the outlet 19b of the second channel 19 of the additional heat exchanger 17 is prone to a liquid-vapor two-phase condition.

4, in order to solve the problem associated with the possible presence of the gas stream in the liquid-vapor two-phase state at the outlet of the additional exchanger 17, Is located above the exchanger 8 and at the outlet 19b of the second channel 19 of the additional heat exchanger 17 the gas stream is directed to the inlet 9a of the first channel 9 of the heat exchanger 8 by gravity It can flow.

In another embodiment illustrated in Figure 5, to avoid the presence of a gas stream in the liquid-vapor two-phase state at the outlet of the additional exchanger 17, the cooling device 16 may include additional heat exchangers (5a, 5b, 5c, 5d), and a second phase heat exchanger (41) in addition to the second phase heat exchanger (17) Transfers heat between streams.

To this end the second additional heat exchanger 41 is connected to the first channel 42 integrated in the steam phase gas collection circuit 6 and to the outlet 43b connected to the vapor phase gas collection circuit 6, And a second channel 43 including an inlet 43a connected to the first channel 43a.

Each of the two additional exchangers 17, 41 is connected to a draw-out circuit 35 via a respective valve 44, 45. Thus, the distribution of the gas stream withdrawn as a liquid phase from the tanks 5a, 5b, 5c, 5d between the two additional exchangers 17, 41 can be adjusted. In particular, the valves 44, 45 are only to be vaporized in the additional heat exchanger 17 when all of the excess gas, i. E. Both the liquid phase gas stream withdrawn from the tanks 5a, 5b, 5c, 5d, The amount of gas that can not be controlled can be guided to the second additional heat exchanger 41. [

Figure 5 shows the nitrogen concentration as a function of the nitrogen concentration of the liquid natural gas for the following natural gas stream:

A steam phase gas stream withdrawn from the tank (curve a);

- a first part (curve b) of the compressed combustible gas stream intended to be conveyed from the installation according to the prior art to the gas consuming members 2, 3 and 4; And

2 in which the flow rate of the gas drawn out from the tanks 5a, 5b, 5c, 5d as a liquid phase and vaporized in the additional heat exchanger 17 is adjusted to optimize the re-liquefaction yield, 3, 4) of the compressed combustible gas stream (curve c).

5 shows the operating conditions under which the vapor phase gas stream withdrawn from the tank has a temperature of -120 DEG C and 70% of the flow of the combustible gas stream returns to the heat exchanger 8 where it is re-liquefied. 5, the atomization of the liquid at the inlet 9a of the first channel 9 of the heat exchanger 8 is effected by the gas consumption < RTI ID = 0.0 > It has been observed that it is possible to substantially reduce the nitrogen concentration of the gas stream intended to be conveyed to the member (s) 2, 3, 4. This is also achieved without deteriorating the re-liquefaction yield.

Figure 6 shows a similar graph when only 50% of the flow of the combustible gas stream to the heat exchanger 8 is returned and resolidified there.

7 shows the difference between the flow rate of the liquid phase gas withdrawn from the tank and the flow rate of the re-liquefied gas as a function of the flow rate of the second portion of the combustible gas stream returned to the heat exchanger 8 for internal re- FIG. The re-liquefying performance qualities in the plant as illustrated in Figure 1 are shown in curve a, and those in the plant as illustrated in Figure 2 are shown in curve b. The operating conditions of the plant are as follows: The nitrogen concentration of the steam phase natural gas collected from the tanks 5a, 5b, 5c, 5d is 20%, the temperature is -140 ° C, The total flow rate of the natural gas stream at the inlet 9a of the channel 9 is 4700 kg per hour and the flow rate of the liquid phase natural gas stream withdrawn from the tank is equal to the flow rate of the second portion of the gas stream circulating in the intermediate circuit 22 Lt; RTI ID = 0.0 > (T1) < / RTI > Figure 7 thus illustrates the increased efficiency of the plant of Figure 2.

Figure 8 shows a first portion of the gas stream intended to be transported to the gas consuming member 2, 3, 4 as a function of the flow rate of the second portion of the combustible gas stream returned to the heat exchanger 8 for internal re- ≪ / RTI > Curve " a " corresponds to the nitrogen content when it is not added to the steam phase gas collection circuit 6 in a prior art facility, i.e., no gas flow is withdrawn from the liquid phase in the liquid phase, Corresponds to the nitrogen content when the gas is drawn out from the tanks 5a, 5b, 5c, and 5d in the liquid phase by the facility as described in Fig. 2, and is vaporized and injected into the vapor phase gas collection circuit 6. The operating conditions of the equipment are the same as those described with reference to Fig. 1 and 2 can significantly reduce the nitrogen concentration of the first portion of the gas stream delivered to the gas consuming member 2, 3, 4, thereby reducing the gas consumption member 2, 3, 4 Lt; RTI ID = 0.0 > of the < / RTI >

9 is a graph showing the difference between the flow rate of the liquid phase gas drawn from the tank and the flow rate of the re-liquefied gas as a function of the flow rate of the second portion of the combustible gas stream returned to the heat exchanger 8. The operating conditions of the equipment are the same as those described with reference to Fig. Curve a corresponds to the remelting performance quality when in a facility according to the prior art, i.e. no gas flow is drawn out of the tank 5a, 5b, 5c, 5d into the liquid phase and added to the steam phase gas collection circuit On the other hand, curve b corresponds to the re-liquefaction performance quality when the gas is drawn out from the tank into the liquid phase by the equipment as described in Fig. 2 and is vaporized and injected into the vapor phase gas collection circuit.

Thus, the use of a cooling device as described in connection with FIG. 2 may enable reducing the nitrogen concentration of the gas stream intended to be delivered to the gas consuming members 2, 3, 4, Does not significantly reduce the redistribution yield by exceeding the flow rate value of the second portion of the combustible gas stream while increasing the re-liquefaction yield to a predetermined flow rate value of the second portion of the stream.

Further, the higher the temperature of the natural gas in the vapor phase drawn out of the tanks 5a, 5b, 5c and 5d, the more the re-liquefaction yield comparison value in the facility as described in Fig. 2, .

10 shows a delivery system 40 for loading / unloading flammable gases such as liquefied natural gas and for forming an interface between a floating or land based installation and a vessel 41 not shown. The vessel 41 has a facility for feeding the combustible gas to the gas consuming member and liquefying the combustible gas as described above. By way of example, the fluid sealing and insulating tanks, which are not shown, are generally in the form of prongs and are mounted on the ship's double hull.

Product delivery is guaranteed by an immersed cryogenic line marked 42. The delivery system 40 that forms the interface between the floating or land based installation and the vessel 41 is adapted to receive the cryogenic line 42 immersed in the flexible transmission pipe 46, 45 and at least one platform 43 that supports the storage / handling gantry 44. Each flexible transmission pipe 46 is intended to be connected to the manifold 47 of the vessel via a connecting module 48. The manifold 47 of the vessel is connected to the tank by a loading / unloading pipeline arranged in the upper deck of the vessel 41 to deliver the liquefied gas from the tank or into the tank.

The main function of the gantry 44 is to enable handling and storage of the transfer portions, i.e., the moving ends of each connecting module 48 and the flexible transfer pipe 46, by the crane and the winch.

Depending on the embodiment, the delivery system comprises three parallel flexible transmission pipes 46, two of which enable delivery of liquefied natural gas between the floating or land based installation and the vessel, while the third delivery The pipe allows gas to be delivered to balance the pressure in the gas head space of the tank of the ship.

The onboard pump of the vessel 41 is used and / or a pump is installed in the onshore infrastructure and / or a pump is installed in the delivery system 40 to create the pressure required for the delivery of the liquefied gas.

Although the present invention has been described in connection with a number of specific embodiments, it is to be understood that the invention is not to be limited in any way, and that all technical equivalents of the described means and combinations thereof, It is clear.

The "include" or "accept" and its conjugations do not exclude the presence of elements or steps other than those listed in the claims.

For this reason, the methods and equipment implemented in accordance with some non-limiting embodiments of the present technology may be expressed as shown in the numbered clauses as follows.

[Item 1] A facility (1) for feeding a combustible gas to a gas consuming member (2, 3, 4) and liquefying the combustible gas, the facility (1) comprising:

- sealed thermal insulation tanks (5a, 5b, 5c, 5d) comprising an interior space intended to be filled with flammable gas in a liquid-vapor two-phase equilibrium state;

(7a, 7b, 7c, 7d) arranged in the interior space of the tanks (5a, 5b, 5c, 5d) and arranged to draw the vapor phase combustible gas stream from the internal spaces of the tanks (5a, 5b, 5c, 5d) A vapor phase gas collection circuit (6) comprising: And

- a heat exchanger (8) comprising a first and a second channel (9, 10) and a heat exchange wall for transferring heat from the second channel (10) to the first channel (9) And the second channel 10 each include an inlet 9a, 10a and an outlet 9b, 10b; The inlet 9a of the first channel 9 being connected to the steam phase gas collection circuit 6 to heat the steam phase combustible gas stream in the heat exchanger 8;

Connected to the outlet (9b) of the first channel (9) of the heat exchanger (8) upstream to compress the combustible gas stream at the outlet of the first channel (9) of the heat exchanger (8) Wherein the three-way connector is capable of conveying a first portion of the combustible gas stream to the gas consuming member (2, 3, 4) and a second portion of the combustible gas stream The second portion of the flammable gas stream to the inlet (10a) of the second channel (10) of the heat exchanger (8); And

Downstream from the return circuit 31 connected upstream to the outlet 10b of the second channel 10 of the heat exchanger 8 via the intermediate circuit 15 and leading to the tanks 5a, 5b, 5c and 5d, An expansion device (14) connected to the expansion device (14) is arranged to reduce the second portion of the combustible gas stream entering from the intermediate circuit (15);

The facility 1 also includes a cooling device 16 including a draw-out circuit 35 which is connected to the tanks 5a, 5b, 5c , 5d) of the liquid phase flammable gas stream; The cooling device 16 includes a liquid phase flammable gas stream withdrawn from the tank and a vapor phase combustible gas stream circulating in the steam phase gas collection circuit 6 and a second portion of the combustible gas stream circulating in the intermediate circuit 15 A liquid phase flammable gas stream arranged to transfer heat between the selected flammable gas streams to be cooled to be withdrawn from the tank and a liquid phase drawn from the tank to cool the combustible gas stream to be cooled using the latent heat of vaporization of the flammable gas stream .

[Clause 2] A facility (1) according to Clause 1, wherein the combustible gas is a gas mixture comprising nitrogen and the cooling device (16) reduces the nitrogen content of the combustible gas stream circulating in the vapor phase gas collection circuit To return the vaporized gas stream of the cooling device 16 to the vapor phase gas collection circuit 6.

[Item 3] The apparatus according to clause 2, wherein the cooling device 16 comprises an additional heat exchanger 17 and the additional heat exchanger is connected to the first and second channels 18, 19 and the first channel 18 And a heat exchange wall for transferring heat to a second channel (19) of the additional heat exchanger (17), wherein each of the first channel (18) and the second channel (19) The first channel 18 being integrated in an intermediate circuit 15 connecting the heat exchanger 8 and the expansion device 14 and the inlet 18b, The outlet 19a of the second channel 19 is connected to the vapor phase gas collection circuit 6. The outlet 19b of the second channel 19 is connected to the vapor phase gas collection circuit 6,

[Item 4] The apparatus according to item 3, wherein the additional heat exchanger (17) is superposed on the heat exchanger (8) and the outlet of the second channel (19) of the additional heat exchanger (17) Is connected to the inlet 9a of the first channel 9 so that a liquid phase gas stream flows from the outlet of the second channel 19 of the additional heat exchanger 17 to the inlet 9a of the first channel 9 of the heat exchanger 8 By gravity.

[Item 5] The apparatus according to item 3, wherein the cooling device 16 includes a first channel 42 integrated into the vapor phase gas collection circuit 6 and an outlet 43b connected to the vapor phase gas collection circuit 6 And a second additional heat exchanger (41) including a second channel (43) including an inlet (43a) connected to the withdrawing circuit (35).

[Item 6] The apparatus according to Clause 2, wherein the cooling device 16 is connected to the inlet 7a, 7b, 7c, 7d of the steam phase gas collection circuit 6 and the first channel 9 of the heat exchanger 8 And includes a chamber 20 and a spray member 21 incorporated in the vapor phase gas collection circuit 6 between the inlet 9a and the spray member connected to the draw circuit 35 of the cooling device 16, 20 to cool the vapor phase gas stream withdrawn from the interior space of the tank and reduce the nitrogen content of the combustible gas stream circulating in the vapor phase gas collection circuit 6.

[Clause 7] The facility according to any one of clauses 2 to 6, wherein the cooling device 16 sucks the liquid phase flammable gas stream through the inlet 27 of the cooling device 16 and delivers it to the withdrawing circuit 35 Lt; RTI ID = 0.0 > 26 < / RTI >

[Item 8] A facility according to clause 7, comprising a gas analyzer (40) capable of delivering a representative measurement of the nitrogen concentration of a first portion of a combustible gas stream, wherein the control unit (36) (2, 3, 4) to ensure a nitrogen concentration in the first portion of the combustible gas stream that is less than the first portion of the combustible gas stream Control signals.

[Clause 9] The apparatus according to clause 8, wherein the control unit (36) is adapted to measure the concentration of the combustible gas stream as a function of a representative measurement of the nitrogen concentration of the first portion of the combustible gas stream and a nominal concentration below the limiting operating concentration of the gas consuming member And to generate a control signal for the pumping device 26 to subordinate the nitrogen concentration of the first portion to the nominal concentration.

[Item 10] The facility according to Clause 8, wherein the control unit 36

A pumping device (26) for subordinating the nitrogen concentration of the first portion of the combustible gas stream to a nominal concentration, as a function of a representative measurement of the nitrogen concentration of the first portion of the combustible gas stream and a nominal concentration of the gas consuming member below the limiting operating concentration A nitrogen concentration preference mode arranged to generate a control signal of the nitrogen concentration; And

A temperature measurement (T1) of a second part of the gas stream circulating in the intermediate circuit (15) at the inlet of the expansion device (14) and a temperature measurement (T1) 26), wherein the re-liquefaction preference mode comprises:

The control unit 36 is arranged to switch from the nitrogen concentration preference mode to the re-liquefaction preference mode as a function of a representative measurement of the nitrogen concentration of the first portion of the combustible gas stream.

[Item 11] The facility according to any one of Items 1 to 10, wherein the expansion device (23) is an expansion valve.

[Item 12] A device according to any one of the above items 1 to 11, which is connected to the return circuit (31) leading from the upstream to the expansion device (14) and from the downstream to the tank on the one hand, and on the other hand, And a phase separator (25) connected to a return pipe (32) connected to the collection circuit (6); The phase separator 25 is arranged to carry the liquid phase of the combustible gas stream to the return circuit 31 and to convey the gas phase of the combustible gas stream to the return pipe 32.

[Item 13] A method of supplying a combustible gas to a gas consuming member by means of the facility according to any one of the items 1 to 12 and liquefying the combustible gas, comprising:

Carrying a vapor phase combustible gas stream from the inlet (7a, 7b, 7c, 7d) of the steam phase gas collection circuit (6) to the inlet (9a) of the first channel (9) of the heat exchanger (8);

Transferring heat from the second channel (10) to the first channel (9) of the heat exchanger (8);

Compressing the combustible gas stream exiting the first channel (9) of the heat exchanger (8);

Conveying a first portion of the compressed combustible gas stream to the gas consuming member 2 and a second portion of the compressed gas stream at the inlet 10a of the second channel 10 of the heat exchanger 8, ; And

Carrying a second portion of the combustible gas stream from the second channel of the heat exchanger (8) through the intermediate circuit (15) to the expansion device (14);

- depressurizing a second portion of the combustible gas stream entering from the intermediate circuit (15);

Conveying at least one liquid phase portion of the second portion of the decompressed combustible gas stream to the tanks (5a, 5b, 5c, 5d);

- withdrawing the liquid phase flammable gas stream from the internal space of the tanks (5a, 5b, 5c, 5d);

Between the liquid phase flammable gas stream withdrawn from the tank and the steam phase gas stream circulating in the steam phase gas collection circuit 6 and the cooled gas stream selected from the second part of the gas stream circulating in the intermediate circuit 15 Transferring heat to vaporize the liquid phase combustible gas stream withdrawn from the tank and cooling the gas stream to be cooled using latent heat of vaporization of the liquid phase combustible gas stream withdrawn from the tank.

[Clause 14] The method according to clause 13, wherein the combustible gas is a gas mixture comprising nitrogen and the vaporized gas stream in the cooling device (16) is returned to the vapor phase gas collection circuit (6).

A method according to clause 14, wherein a variable representing the nitrogen concentration of the first portion of the combustible gas stream is measured and the flow rate of the liquid phase combustible gas stream circulating in the withdrawing circuit (35) of the cooling device (16) Is adjusted as a function of the variable representing the nitrogen concentration of the first portion of the combustible gas stream.

[Item 16] The method according to clause 15, wherein the flow rate of the liquid phase combustible gas stream circulating in the withdrawing circuit (35) of the cooling device (16) is a function of a nominal concentration and a variable representing the nitrogen concentration of the first portion of the combustible gas stream Is adjusted to subordinate the nitrogen concentration of the first portion of the combustible gas stream to the nominal concentration.

[Item 17] A ship (40) including the facility (1) according to any one of the items 1 to 12.

[Clause 18] A method for loading or unloading a vessel (40) according to clause 17, wherein the combustible gas is delivered through a cryogenic transfer pipe (42, 46) from a floating or land based storage facility to the vessel's tank or vice versa.

[Clause 19] A system for delivering flammable gas comprising: a vessel according to clause 17; a cryogenic transfer pipe (42, 46) arranged to connect a tank installed in the ship's hull to a floating or land based storage facility; Or a pump for driving the combustible gas stream through an insulated pipeline from a land-based storage facility to a vessel's tank or vice versa.

Claims (16)

An apparatus for feeding a combustible gas to a gas consuming member and liquefying the combustible gas:
A sealed thermal insulation tank comprising an interior space intended to be filled with flammable gas in a liquid-vapor two-phase equilibrium state;
A vapor phase gas collection circuit comprising an inlet arranged to draw a vapor phase combustible gas stream emerging from the interior space of the tank and from the interior space of the tank; And
A heat exchanger comprising a heat exchange wall for transferring heat from the first and second channels to the first channel, the first channel and the second channel each comprising an inlet and an outlet; The inlet of the first channel being connected to the steam phase gas collection circuit (6) to heat the steam phase combustible gas stream in the heat exchanger;
A compressor connected downstream of the three-chamber connector and connected to the outlet of the first channel of the heat exchanger upstream to compress the combustible gas stream at the outlet of the first channel of the heat exchanger, A portion of the combustible gas stream capable of carrying a second portion of the combustible gas stream to the inlet of a second channel of the heat exchanger to cool the second portion of the combustible gas stream; And
An expansion device connected upstream from the outlet of the second channel of the heat exchanger through the intermediate circuit to the return circuit leading to the tank and connected downstream, the expansion device being arranged to reduce the second portion of the combustible gas stream entering the intermediate circuit -
The apparatus comprising:
The facility 1 further comprises a cooling device comprising a draw-out circuit, said draw-out circuit comprising an inlet arranged to draw a liquid phase flammable gas stream of the internal space of the tank as it appears in the internal space of the tank; The cooling device includes a liquid phase flammable gas stream withdrawn from the tank and a steam phase combustible gas stream circulating in the steam phase gas collection circuit and a heat To cool the flammable gas stream to be cooled using a latent heat of vaporization of the liquid phase flammable gas stream drawn from the tank and withdrawn from the tank and withdrawn from the tank. 2. The method of claim 1, wherein the combustible gas is a gas mixture comprising nitrogen and the cooling device is operable to reduce the nitrogen content of the combustible gas stream circulating in the steam phase gas collection circuit to a vapor phase gas collection An arrangement (1) arranged to convey to a circuit. 3. The apparatus of claim 2 wherein the cooling device includes a chamber and a spray member integrated in a vapor phase gas collection circuit between an inlet of the steam phase gas collection circuit and an inlet of the first channel of the heat exchanger, A device connected to the circuit and arranged to spray a liquid phase combustible gas into the chamber to cool the vapor phase gas stream withdrawn from the interior space of the tank and to reduce the nitrogen content of the combustible gas stream circulating in the vapor phase gas collection circuit. 4. A system according to claim 2 or 3, wherein the cooling device (16) comprises a pumping device (26) for sucking the liquid phase flammable gas stream through an inlet (27) of the cooling device (16) ≪ / RTI > 5. The apparatus of claim 4, comprising a gas analyzer capable of delivering representative measurements of the nitrogen concentration of the first portion of the combustible gas stream, wherein the control unit is configured to determine a nitrogen concentration of the first portion of the combustible gas stream that is less than the limiting operating concentration of the gas consuming member Of the first portion of the combustible gas stream to be conveyed to the gas consuming member to assure the nitrogen concentration of the combustible gas stream. 6. The method of claim 5, wherein the control unit is operative to determine a nitrogen concentration of the first portion of the combustible gas stream as a function of a nominal concentration of the first portion of the combustible gas stream and a nominal concentration of the gas consuming member below a limiting operating concentration, To generate a control signal for the pumping device. 6. The apparatus of claim 5, wherein the control unit
Control of the pumping device to subordinate the nitrogen concentration of the first portion of the combustible gas stream to the nominal concentration as a function of a representative measurement of the nitrogen concentration of the first portion of the combustible gas stream and a nominal concentration less than the limiting operating concentration of the gas consuming member A nitrogen concentration preference mode arranged to generate a signal; And
- generating a control signal for the pumping device to arrange the temperature (T1) for the nominal temperature as a function of the nominal temperature and a temperature measurement (T1) of the second part of the gas stream circulating in the intermediate circuit of the inlet of the expansion device A re-liquefaction priority mode;
Wherein the control unit is arranged to switch from a nitrogen concentration preference mode to a re-liquefaction preference mode as a function of a representative measurement of the nitrogen concentration of the first portion of the combustible gas stream. 4. The installation according to any one of claims 1 to 3, wherein the expansion device is an expansion valve. 4. A device as claimed in any one of the preceding claims, which is connected to a return pipe leading from the upstream to the expansion device and from the downstream to the tank on the one hand and to a return pipe connected to the vapor phase gas collection circuit on the other A phase separator; Wherein the phase separator is arranged to carry the liquid phase of the combustible gas stream to the return circuit and convey the gas phase of the combustible gas stream to the return pipe. A method for supplying a combustible gas to a gas consuming member and liquefying the combustible gas by an apparatus according to claim 1,
Conveying the vapor phase combustible gas stream from the inlet of the steam phase gas collection circuit to the inlet of the first channel of the heat exchanger;
Transferring heat from the second channel to the first channel of the heat exchanger;
Compressing the combustible gas stream exiting the first channel (9) of the heat exchanger;
Conveying the first portion of the compressed combustible gas stream to the gas consuming member and returning the second portion of the compressed gas stream to the inlet of the second channel of the heat exchanger;
Conveying a second portion of the combustible gas stream from the second channel of the heat exchanger through the intermediate circuit to the expansion device;
- depressurizing a second portion of the combustible gas stream entering from the intermediate circuit;
Conveying at least one liquid phase portion of the second portion of the reduced pressure combustible gas stream to the tank;
Withdrawing a liquid phase flammable gas stream from the interior space of the tank;
Transferring heat between the liquid phase flammable gas stream withdrawn from the tank and the steam phase gas stream circulating in the steam phase gas collection circuit and the cooled gas stream selected from the second portion of the gas stream circulating in the intermediate circuit, Vaporizing the withdrawn liquid phase combustible gas stream and cooling the gas stream to be cooled using latent heat of vaporization of the liquid phase combustible gas stream withdrawn from the tank. 11. The method of claim 10 wherein the combustible gas is a gas mixture comprising nitrogen and the vaporized gas stream in the cooling device is returned to the vapor phase gas collection circuit. 12. The method of claim 11, wherein a variable indicative of the nitrogen concentration of the first portion of the combustible gas stream is measured and wherein the flow rate of the liquid phase combustible gas stream circulating in the withdrawal circuit of the cooling device is greater than the nitrogen concentration of the first portion of the combustible gas stream As a function of the variables representing the variables. 13. The method of claim 12, wherein the flow rate of the liquid phase combustible gas stream circulating in the withdrawal circuit of the cooling device is a function of the nominal concentration and the nitrogen concentration of the first portion of the flammable gas stream Wherein the concentration is adjusted to subordinate to the nominal concentration. A ship containing the installation according to paragraph 1. A method for loading or unloading a vessel according to claim 14, wherein the combustible gas is delivered through a pipeline insulated from a floating or land based storage facility to the tank of the vessel or vice versa. Systems for the delivery of flammable gases, including ships in accordance with paragraph 14, insulated pipelines arranged to connect tanks on board the ship's hull to floating or land based storage facilities, and floating or land based storage facilities to vessels' tanks And a pump for driving the combustible gas stream through the insulated pipeline.

Images