KR20220048745A - treatment system of liquefied gas and vessel having same - Google Patents

Abstract

The present invention relates to a liquefied gas processing system and a ship including the same. The liquefied gas processing system includes: a heat exchanger heating a liquefied gas, supplied from a liquefied gas storage tank, using latent heat of a thermal medium; and a thermal medium circulation line heating the thermal medium discharged from the heat exchanger to circulate the thermal medium to the heat exchanger, wherein the thermal medium circulation line includes: a thermal medium supply line supplying a gaseous thermal medium to the heat exchanger; a thermal medium recovery line receiving a liquefied thermal medium liquefied and discharged by the heat exchanger; a thermal medium heater provided between the thermal medium supply line and the thermal medium recovery line and gasifying the liquefied thermal medium; a start-up line provided so as to connect the upstream of the heat exchanger to the downstream thereof and flowing the thermal medium to the thermal medium supply line when the heat exchanger is initially operated; and a pump provided upstream of a point where the start-up line branches off from the thermal medium recovery line, and forcibly supplying the thermal medium to the start-up line when the heat exchanger is initially operated. When the heat exchanger is normally operated, the thermal medium is circulated by the head pressure of the liquefied thermal medium discharged from the heat exchanger. The present invention can enhance heat transfer efficiency and heat exchange efficiency between the liquefied gas and the thermal medium.

Description

Liquefied gas treatment system and vessel including the same {treatment system of liquefied gas and vessel having same}

The present invention relates to a liquefied gas processing system and a ship including the same.

In general, liquefied natural gas (Liquefied Nature Gas) is a clean fuel and is known to have more abundant reserves than petroleum, and its usage is rapidly increasing with the development of mining and transport technology. In such LNG, methane, the main component, is generally stored in a liquid state by lowering the temperature to -162 or less under 1 atm. The volume of liquefied methane is about 1/600 of the volume of gaseous methane, which is a standard state, and the specific gravity is 0.42, which is about one-half of the weight of crude oil.

LNG is liquefied due to its ease of transport and vaporized at the place of use after transport. In regions with stable LNG demand, LNG storage and regasification systems are installed onshore, but countries with unstable demand or risks of natural disasters and terrorism are concerned about installing LNG vaporization facilities onshore.

For this reason, instead of the conventional liquefied natural gas regasification system installed on land, a ship that supplies vaporized natural gas to land by installing a regasification device on an LNG carrier that transports liquefied natural gas (LNG FSRU, for example) is in the spotlight.

Currently, in a ship including an LNG regasification device, various research and development for efficiently driving a heat source supply device for gasifying LNG are being conducted.

The present invention was created to solve the problems of the prior art as described above, and an object of the present invention is a liquefied gas processing system capable of efficiently supplying liquefied gas to consumers by processing liquefied gas according to the requirements of the consumers, and a ship including the same is to provide

The liquefied gas processing system according to an embodiment of the present invention is a heat exchanger that heats liquefied gas supplied from a liquefied gas storage tank using latent heat of a heat exchanger, and heats the heat medium discharged from the heat exchanger and circulates to the heat exchanger and a heat medium circulation line, wherein the heat medium circulation line includes a heat supply line for supplying gaseous heat to the heat exchanger, a heat recovery line for receiving liquid heat liquefied and discharged from the heat exchanger, the heat supply line and the heat medium A heat medium heater provided between the recovery lines and vaporizing the liquid heat medium, a startup line provided to connect the upstream and downstream of the heat medium heater, and flowing heat to the heat medium supply line when the heat exchanger is initially operated, and the a pump provided upstream of a branching point of the startup line in the heat recovery line, and forcibly supplying heat to the startup line when the heat exchanger is initially operated, and the heat exchanger during normal operation of the heat exchanger It is characterized in that the fruit is circulated by the head pressure of the liquid fruit discharged from the

Specifically, when the heat exchanger is normally operated, the gaseous heat from the heat supply line may be supplied to the heat exchanger by the pressure of the liquid heat flowing in the heat recovery line.

Specifically, the pump may forcibly supply the heat medium to the heat medium circulation line when the heat exchanger malfunctions or the head pressure of the liquid heat medium discharged from the heat exchanger decreases to a predetermined value or less.

Specifically, a plurality of the pumps may be provided in parallel on the heat medium recovery line.

Specifically, the plurality of pumps may have different capacities.

Specifically, the liquefied gas treatment system further includes a control unit for determining whether to operate the pump, the heat medium circulation line is provided at a higher position than the pump in the vertical direction, and the heat medium discharged from the heat exchanger It further includes a heat drum for storing the heat, the control unit may control the pump according to the water level of the heat stored in the heat drum.

Specifically, the controller may control the pump so that the water level of the heat medium stored in the heat medium drum provides more than the head pressure required for circulation of the liquid heat medium during normal operation of the heat exchanger.

Specifically, the heat medium circulation line may further include a bypass line bypassing the pump.

Specifically, in the heat medium circulation line, a plurality of the heat exchangers are provided in parallel, a plurality of the heat medium heaters are provided in parallel, and the heat medium discharged from each of the plurality of heat exchangers is joined to each of the plurality of heat medium heaters. can transmit

A ship according to an embodiment of the present invention is characterized in that it includes the liquefied gas processing system.

The liquefied gas processing system according to the present invention can effectively improve the heat transfer efficiency and heat exchange efficiency between the liquefied gas and the heat medium.

The liquefied gas processing system according to the present invention can improve the efficiency of facility operation.

The liquefied gas processing system according to the present invention can stably supply liquefied gas to the consumer in accordance with the requirements of the consumer.

1 is a conceptual diagram of a liquefied gas processing system according to a first embodiment of the present invention.
2 is a graph of a heat flow rate versus temperature of a heat exchanger in a conventional liquefied gas treatment system.
3 is a graph of the heat flow rate versus temperature of the first heat exchanger and the second heat exchanger of the liquefied gas treatment system of the present invention.
4 is a conceptual diagram of a liquefied gas processing system according to a third embodiment of the present invention.
5 is a conceptual diagram of a liquefied gas processing system according to a fourth embodiment of the present invention.
6 is a conceptual diagram of a liquefied gas processing system according to a fifth embodiment of the present invention.
7 is a conceptual diagram of a liquefied gas processing system according to a sixth embodiment of the present invention.
8 is a conceptual diagram of a liquefied gas processing system according to a seventh embodiment of the present invention.
9 is a conceptual diagram of a liquefied gas processing system according to an eighth embodiment of the present invention.
10 is a conceptual diagram of a liquefied gas processing system according to a ninth embodiment of the present invention.
11 is a conceptual diagram of a liquefied gas processing system according to a tenth embodiment of the present invention.

The objects, specific advantages and novel features of the present invention will become more apparent from the following detailed description and preferred embodiments taken in conjunction with the accompanying drawings. In the present specification, in adding reference numbers to the components of each drawing, it should be noted that only the same components are given the same number as possible even though they are indicated on different drawings. In addition, in describing the present invention, if it is determined that a detailed description of a related known technology may unnecessarily obscure the gist of the present invention, the detailed description thereof will be omitted.

Hereinafter, it should be noted that high pressure (HP), low pressure (LP: low pressure), high temperature, and low temperature are relative and do not represent absolute values.

Hereinafter, liquefied gas may be used to encompass all gas fuels that are generally stored in a liquid state, such as LNG or LPG, ethylene, ammonia, etc. can This can be applied to boil-off gas as well. In addition, for convenience, LNG can be used to encompass both NG (Natural Gas) in a liquid state as well as NG in a supercritical state. there is.

Hereinafter, the liquefied gas processing system of the present invention will be described, and the present invention includes a liquefied gas processing system and a ship having the same. At this time, it should be noted that the vessel may be a general commercial vessel that loads cargo other than liquefied gas in addition to the liquefied gas carrier, and furthermore, it is an expression that encompasses all marine structures such as FSRU and FLNG, which are not commercial vessels.

Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings.

Hereinafter, the liquefied gas processing system of the present invention will be described in detail with reference to FIGS. 1 to 9 .

1 is a conceptual diagram of a liquefied gas processing system according to a first embodiment of the present invention.

Referring to FIG. 1 , the liquefied gas processing system 1 according to the first embodiment of the present invention includes a liquefied gas storage tank 10 , a liquefied gas supply line L10 , a first heat exchanger 30 , and a second It includes a heat exchanger 40, a first heat medium circulation line (L20), and a second heat medium circulation line (L30).

In the present invention, valves (not shown) capable of adjusting the opening degree may be installed in each line, and the flow of fluids such as liquefied gas, boil-off gas, heat medium, etc. may be controlled according to the opening degree of each valve.

The liquefied gas supply line (L10) connects the liquefied gas storage tank (10) and the customer (100), and includes a buffer tank (20), a boosting pump (21), a first heat exchanger (30), and a second heat exchanger ( 40) is provided, and the liquefied gas stored in the liquefied gas storage tank 10 is supplied to the buffer tank 20 through the pump 11 and then supplied to the boosting pump 21, and the boosting pump 21 to high pressure. The compressed liquefied gas may be heat-exchanged in the first heat exchanger 30 and the second heat exchanger 40 to be supplied to the consumer 100 .

Hereinafter, individual components organically formed and implemented in the liquefied gas processing system 1 will be described.

The liquefied gas storage tank 10 stores the liquefied gas to be supplied to the consumer 100 . At this time, the liquefied gas storage tank 10 may store the liquefied gas in a liquid state, and may have a pressure tank shape.

Here, the liquefied gas storage tank 10 is disposed inside the hull, and may be formed in four, for example, in front of the engine room. In addition, the liquefied gas storage tank 10 is, for example, a membrane type tank, but is not limited thereto, and the type is not particularly limited to various types, such as an independent tank.

In the liquefied gas storage tank 10 , a cofferdam (not shown) may be disposed between each liquefied gas storage tank 10 , and a cofferdam may also be disposed between the engine room and the liquefied gas storage tank 10 . can

A pump 11 may be provided in the liquefied gas storage tank 10 , and the liquefied gas stored in the liquefied gas storage tank 10 may be withdrawn through the pump 11 .

At this time, the pump 11 may be a submersible pump when provided inside the liquefied gas storage tank 10 . In addition, when the pump 11 is installed outside the liquefied gas storage tank 10, it may be provided at a position inside the hull lower than the water level of the liquefied gas stored in the liquefied gas storage tank 10, and may be a centrifugal pump. there is.

The buffer tank 20 may be provided in the liquefied gas supply line L10 to receive the liquefied gas from the liquefied gas storage tank 10 and temporarily store it.

Specifically, the buffer tank 20 may receive the liquefied gas stored in the liquefied gas storage tank 10 from the pump 11 through the liquefied gas supply line L10, and may be liquefied by temporarily storing the supplied liquefied gas. Gas may be separated into a liquid phase and a gas phase, and the separated liquid phase may be supplied to the boosting pump 21 .

That is, the buffer tank 20 temporarily stores the liquefied gas, separates the liquid phase and the gas phase, and supplies the complete liquid phase to the boosting pump 21 , and the boosting pump 21 provides an effective suction head (Net Positive Suction Head; NPSH). ) is satisfied, thereby preventing cavitation in the boosting pump 21 .

In addition, the buffer tank 20 may be connected to a boil-off gas supply line (not shown) to receive the boil-off gas generated from the liquefied gas storage tank 10 and temporarily store it.

Specifically, the buffer tank 20 may receive the BOG generated in the liquefied gas storage tank 10 from a BOG compressor (not shown) through a BOG supply line and temporarily store the BOG.

Through this, the buffer tank 20 may heat-exchange the temporarily stored liquefied gas supplied from the liquefied gas supply line L10 and the temporarily stored boil-off gas supplied from the boil-off gas supply line to each other to re-condense them. Here, the buffer tank 20 may be formed in a pressure vessel type capable of withstanding pressure, and may withstand a pressure of 6 to 8 bar or 6 to 15 bar.

Accordingly, the buffer tank 20 receives the boil-off gas and liquefied gas at a pressure of about 6 to 8 bar (or even 6 to 15 bar) through the boil-off gas compressor and the pump 11, and maintains the pressure. By re-condensing, the liquefied gas is supplied to the boosting pump 21 to lower the compression load of the boosting pump 21 .

The boosting pump 21 may be provided between the buffer tank 20 and the first heat exchanger 30 on the liquefied gas supply line L10 and the liquefied gas or buffer tank 20 supplied from the pump 11 . It can be supplied to the first heat exchanger 30 by pressurizing the liquefied gas supplied from the 50 to 120 bar.

The boosting pump 21 may pressurize the liquefied gas according to the pressure required by the demand 100 , and may be configured as a centrifugal pump.

The first heat exchanger 30 may heat the liquefied gas transferred to the first heat exchanger 30 by using the latent heat of the first heat medium circulating in the first heat medium circulation line L20 .

That is, the first heat exchanger 30 is at least parallel to the liquefied gas supply line L10 and a flow path (not shown) through which low-temperature liquefied gas flows, and the first heat medium circulation line L20 and parallel to the high-temperature product. 1 A flow path (not shown) through which the fruit flows may be provided.

At this time, the first heat medium may be supplied to the first heat exchanger 30 in a gaseous state, and the first heat exchanged in the first heat exchanger 30 may be discharged after a phase change into a liquid state. That is, the first heat exchanger 30 may heat the liquefied gas by using the latent heat of the first heat medium.

When the pressure of the liquefied gas supplied to the first heat exchanger 30 is less than the critical pressure of the liquefied gas, the liquefied gas in the first heat exchanger 30 may be vaporized through latent heat of the first heat exchanger. On the other hand, when the pressure of the liquefied gas supplied to the first heat exchanger 30 is equal to or greater than the critical pressure of the liquefied gas, the liquefied gas is supplied to the first heat exchanger 30 in a supercritical state, and the liquefied gas as the supercritical fluid is It can be heated through the latent heat of the first fruit.

2 is a graph of a heat flow rate versus temperature of a heat exchanger in a conventional liquefied gas treatment system. Specifically, Fig. 2 (a) is a graph showing the temperature versus heat flow rate of the heat exchanger when the pressure of the liquefied gas supplied to the heat exchanger is less than the critical pressure, and Fig. 2 (b) is the pressure of the liquefied gas supplied to the heat exchanger. It is a graph showing the temperature versus the heat flow rate of the heat exchanger when the critical pressure is higher than the critical pressure.

Referring to (a) of Figure 2, when the pressure of the liquefied gas supplied to the heat exchanger for exchanging heat with the liquefied gas is less than the critical pressure, the liquefied gas is heated through heat exchange with the heat and is in a liquid state at about -80 ° C. A phase change can occur from the to the gaseous state. In addition, the gaseous fruit may be phase-changed to a liquid state at about -0 °C. At this time, as there is a phase change section of the liquefied gas in the heat exchanger, in the vicinity of the section where the heat medium is phase changed, the temperature of the liquefied gas in the heat exchanger becomes higher than the temperature of the heat exchanger. .

On the other hand, referring to FIG. 2B , when the pressure of the liquefied gas supplied to the heat exchanger is equal to or greater than the critical pressure, the liquefied gas is heated in the heat exchanger in a supercritical state without a phase change. At this time, as the phase change of the liquefied gas does not occur in the heat exchanger, a section in which the temperature of the liquefied gas becomes higher than the temperature of the heat medium is reversed may be formed in the heat exchanger. When a temperature reversal phenomenon occurs in which the temperature of the liquefied gas becomes higher than the temperature of the heat medium, a problem may occur that the liquefied gas is not heated by the heat medium.

Accordingly, in the first heat exchanger 30 in the present invention, when the pressure of the liquefied gas supplied to the first heat exchanger 30 is equal to or greater than the critical pressure, the temperature of the liquefied gas in the first heat exchanger 30 is that of the first heat exchanger. It may be provided so as to be prevented from becoming higher than the temperature.

Figure 3 is a graph of the heat flow rate versus temperature of the first heat exchanger and the second heat exchanger of the liquefied gas treatment system of the present invention.

Referring to FIG. 3 , when liquefied gas having a pressure greater than or equal to the critical pressure is supplied to the first heat exchanger 30, the first heat exchanger ( 30) may be provided to exchange heat with the liquefied gas and the first fruit.

On the other hand, when the pressure of the liquefied gas supplied to the first heat exchanger 30 is less than the critical pressure of the liquefied gas, the liquefied gas in the first heat exchanger 30 changes from a liquid state to a gaseous state as described above. Since there is a change section, the liquefied gas may be vaporized through the first heat medium without a temperature reversal phenomenon.

Therefore, in the present invention, even when the pressure of the liquefied gas supplied to the first heat exchanger 30 is less than or equal to or greater than the critical pressure, it is possible to effectively heat the liquefied gas by using the latent heat of the first heat exchanger without temperature reversal. .

In addition, as will be described later, the second heat exchanger 40 heats the liquefied gas using the sensible heat of the second heat medium, so that even when the liquefied gas is in a supercritical state, the temperature of the liquefied gas in the second heat exchanger 40 is It can effectively heat the liquefied gas without reversing the temperature higher than the temperature of the fruit.

A first heat exchanger 30 , a heat medium drum 31 , and a first heat medium heater 32 may be provided in the first heat medium circulation line L20 , and the first heat medium in the liquid phase is transferred from the first heat medium heater 32 . It may be vaporized to be in a gaseous state, and the first heat medium in a gaseous state may be heat-exchanged with liquefied gas in the first heat exchanger 30 to be phase-changed into a liquid state. The liquid first heat medium discharged from the first heat exchanger 30 is temporarily stored in the heat medium drum 31 through the heat medium recovery line L22, and the first heat medium in the liquid phase is delivered to the first heat exchanger 32 can

The first heat medium heater 32 receives the first heat medium in liquid form from the heat medium drum 31, vaporizes the first heat medium, and transfers the first heat medium in the gas phase to the first heat exchanger 30 through the heat medium supply line L21. can be supplied with At this time, the first heat medium heater 32 may vaporize the liquid first heat medium using seawater.

That is, the first heat medium heater 32 has at least a flow path (not shown) through which a liquid first heat medium flows in parallel with the first heat medium circulation line (L20), and a flow path through which seawater flows (not shown). can do.

In the first heat medium heater 32, the liquid first heat medium is heated through seawater, and in the process of heating the first heat medium, a temperature reversal phenomenon in which the temperature of the first heat medium becomes higher than the temperature of the seawater may occur.

At this time, by reducing the supply flow rate of the first heat medium supplied to the first heat medium heater 32 to lower the equilibrium temperature and pressure condition of the heat medium circulation system, the temperature of the first heat medium in the first heat medium heater 32 is seawater It is possible to prevent the temperature reversal phenomenon that is higher than the temperature of .

A second heat exchanger 40 , a second heat medium heater 41 , and a heat medium pump 42 may be provided in the second heat medium circulation line L30 , and the liquid second heat medium is transferred from the second heat medium heater 41 . The second heat medium heated while maintaining the liquid phase may be supplied to the second heat exchanger 40 via the heat medium pump 42 .

The second heat exchanger 40 may heat the liquefied gas transferred to the second heat exchanger 40 by using the sensible heat of the second heat medium circulating in the second heat medium circulation line L30 .

That is, the second heat exchanger 40 is at least parallel to the liquefied gas supply line L10 and a flow path (not shown) through which liquefied gas flows, and a second heat medium circulation line L30 and a high temperature second heat medium. may be provided with a flow path (not shown) through which is flowed.

At this time, the second heat medium may be supplied to the second heat exchanger 40 in a liquid state, and may be discharged in a liquid state after heat exchange in the second heat exchanger 40 . That is, the second heat exchanger 40 may heat the liquefied gas by using the sensible heat of the second heat medium.

When the liquefied gas pressurized above the critical pressure is delivered to the first heat exchanger 30 and the second heat exchanger 40, the first The heat exchanger 30 may be provided, and the second heat exchanger 40 may be provided in a section where temperature reversal may occur. In this case, the second heat medium in the second heat exchanger 40 exchanges heat with the liquefied gas without a phase change, thereby preventing temperature reversal in the second heat exchanger 40 from occurring.

Therefore, in the present invention, the liquefied gas stored in the liquefied gas storage tank 10 can be effectively heat-exchanged with the heat circulating in the first heat medium circulation line L20 and the second heat medium circulation line L30, and can be supplied to the consumer 100 there is.

The second heat medium heater 41 may receive the second heat medium in the liquid phase discharged through heat exchange in the second heat exchanger 40 to maintain the liquid phase and heat the second heat medium. At this time, the second heat medium heater 41 may heat the liquid second heat medium using seawater.

That is, the second heat medium heater 41 has at least a flow path (not shown) through which a liquid second heat medium flows parallel to the second heat medium circulation line L30 and a flow path (not shown) through which seawater flows. can do.

The liquid second heat medium heated by the second heat medium heater 41 is supplied to the heat medium pump 42 , and the heat medium pump 42 may pressurize the liquid second heat medium and supply it to the second heat exchanger 40 . . At this time, as the liquid second heat medium is pressurized through the heat pump 42 , it can be stably supplied to the second heat exchanger 40 . In addition, the heat pump 42 may pressurize the second heat medium to a pressure at which the second heat medium can effectively exchange heat with the liquefied gas in the second heat exchanger 40 .

The liquefied gas processing system 1 may include an expansion drum 50 . The expansion drum 50 is branched and connected to the second heat medium circulation line L30, is disposed above the second heat medium heater 41 and the heat medium pump 42, and the pressure in the second heat medium circulation line L30 change can be compensated for. The expansion drum 50 may be provided in the pressure compensation line L40 branched between the heat heat pump 42 of the second heat medium circulation line L30 and the second heat exchanger 40 .

When overpressure occurs in the second heat medium circulation line L30, the liquid second heat medium flowing in the second heat medium circulation line L30 may be introduced into the expansion drum 50 along the pressure compensation line L40. . On the other hand, when a low pressure occurs in the second heat medium circulation line L30, the liquid second heat medium temporarily stored in the expansion drum 50 flows into the second heat medium circulation line L30 along the pressure compensation line L40. can

By compensating the pressure of the second heat medium circulation line L30 by the expansion drum 50, it is possible to stabilize the heat medium system of the second heat medium circulation line L30, and the second heat exchanger 40 and the second heat medium heater ( 41) can be prevented from lowering the heat exchange efficiency.

The liquefied gas treatment system 1 may include a heat medium storage tank 60 and a heat medium transfer line L50 connecting the first heat medium circulation line L20 and the second heat medium circulation line L30. A heat transfer pump 61 may be provided in the heat transfer line L50, the heat stored in the heat storage tank 60 is pressurized by the heat transfer pump 61, and the first heat through the heat transfer line L50 It may be transmitted to the circulation line (L20) and the second heat medium circulation line (L30).

The first fruit circulating in the first heat medium circulation line L20 and the second heat medium circulating in the second heat heat circulation line L30 may have the same composition. By using the first heat medium and the second heat medium in the same composition, it is possible to more stably and easily supply and circulate the fruit to the first heat medium circulation line L20 and the second heat medium circulation line L30.

The first fruit and the second fruit may be mixed fruit. By using the mixed heat medium as the first heat medium, the first heat medium in the liquid phase can be more easily phase-changed into the gas phase in the first heat medium heater 32 , and the first heat medium in the gas phase is more easily changed in the first heat exchanger 30 than in the first heat exchanger 30 . It can be easily changed into a liquid phase.

The mixed fruit may be a fruit containing the R134a series, preferably R421a, and most preferably R407c.

Table 1 below shows the physical properties of the glycol-water fruit and the R407c mixed fruit used in the present invention.

Properties glycol-water R407c Temperature Range 10℃->-10℃ 10℃->-20℃ Design Pressure 10 barg 18 barg Operation Pressure ~7 barg ~ 13 barg Flow Rate 434.9 m ³ /hr 581.9 m ³ /hr Viscosity 7.47 cP 0.26 cP Heat Capacity 69 kJ/kg 242 kJ/kg

Referring to Table 1, the R407c mixed fruit used in the present invention has a larger heat capacity than glycol water, so the heat cycle speed in the first heat medium circulation line (L20) and the second heat medium circulation line (L30) is increased. can be reduced. In addition, since the R407c mixed heat medium has a lower viscosity than glycol water, it is possible to effectively reduce frictional loss due to heat in the first heat medium circulation line L20 and the second heat medium circulation line L30.

Therefore, in the present invention, by using a mixed heat medium including R134a series as a heat medium circulating in the heat medium circulation line, it is possible to reduce the power consumption of the heat medium circulation line, thereby reducing the CAPEX and OPEX of the liquefied gas treatment system (1).

The consumer 100 may receive and consume the liquefied gas heated by the first heat exchanger 30 and the second heat exchanger 40 . Here, the customer 100 is a liquefied gas vaporized in the first heat exchanger 30 and heated in the second heat exchanger 40 , or a second heated in the first heat exchanger 30 and the second heat exchanger 40 . The liquefied gas in a critical state may be supplied and used, and may be a land terminal installed on land or an offshore terminal installed floating on the sea.

The first heat medium circulation line L20 and the second heat heat circulation line L30 may be independently provided. A first heat medium circulation line (L20) for supplying and circulating a first heat medium to the first heat exchanger (30) and a second heat medium circulation line (L30) for supplying and circulating a second heat medium to the second heat exchanger (40) By providing separately, even if the pressure, the presence or absence of a phase change, flow rate, the amount of heat required during heat exchange, etc. of the heat medium supplied to the first heat exchanger 30 and the second heat exchanger 40, respectively, are different, according to this, the heat medium is stably and efficiently can be supplied and circulated.

The liquefied gas processing system (1) according to the second embodiment of the present invention includes a liquefied gas storage tank (10), a heat exchanger (30), a heat medium circulation line (L20), a heat medium drum (31), and a heat medium heater (32) includes

Each of the heat exchanger 30, the heat medium circulation line L20, the heat medium drum 31, and the heat medium heater 32 in the liquefied gas processing system 1 according to the second embodiment of the present invention, the first embodiment The first heat exchanger 30, the first heat medium circulation line (L20), the heat medium drum 31, and the first heat medium heater 32 in the liquefied gas treatment system 1 according to may be the same, respectively.

Hereinafter, the present embodiment will be mainly described on the points that are different from the previous embodiment, and the parts omitted from the description will be replaced with the previous content. Note that this is also the case for the embodiments to be described later.

The heat exchanger 30, the heat drum 31, and the heat heater 32 are provided in the heat medium circulation line (L20), and are sequentially located at different heights in the vertical direction, so that the heat medium in the heat medium circulation line (L20) can be circulated smoothly.

The heat exchanger 30 may receive vapor-phase heat-exchange with the liquefied gas, and then discharge the cooled liquid-phase heat-exchange with the liquefied gas. The heat drum 31 is provided below the heat exchanger 30 , and the liquid heat discharged from the heat exchanger 30 may be introduced into the heat drum 31 by gravity and the load of the heat medium.

The heat medium drum 31 may temporarily store the liquid heat medium discharged from the heat exchanger 30 , and transfer the liquid heat medium to the heat medium heater 32 . At this time, the heat medium heater 32 is provided below the heat medium drum 31 , and the liquid heat discharged from the heat medium drum 31 may be transferred to the heat medium heater 32 by gravity and the load of the heat medium.

The heat medium heater 32 may vaporize the liquid heat received from the heat medium drum 31 using seawater. At this time, the liquefied gas vaporized in the heat medium heater 32 is discharged from the heat medium heater 32 by the head pressure of the liquid heat transferred from the heat medium drum 31 to the heat medium heater 32 , and in the heat medium heater 32 . The discharged gaseous heat may be supplied to the heat exchanger 30 .

That is, the heat medium can be smoothly circulated in the heat medium circulation line L20 without a separate pressurizing device such as a pump for circulating the heat medium. Therefore, in this embodiment, by reducing the installation cost and operating cost of the heat medium circulation line (L20), it is possible to effectively lower the CAPEX and OPEX of the liquefied gas processing system (1).

The liquefied gas processing system 1 includes a second heat exchanger 40 for heating the liquefied gas heat-exchanged in the heat exchanger 30 , and a second heat medium circulation line L30 for circulating a heat medium in the second heat exchanger 40 . may include The second heat medium circulation line L30 may be provided with a second heat medium heater 41 and heat pump 42 , and the heat pump 42 may be located above the second heat medium heater 41 .

The second heat exchanger 40 may receive the liquid heat medium and exchange heat with the liquefied gas, and then discharge the cooled liquid heat through the heat exchange with the liquefied gas. The liquid heat medium discharged from the second heat exchanger 40 may be transferred to the second heat medium heater 41 by gravity and the load of the heat medium.

The second heat medium heater 41 may use seawater to heat the liquid heat medium cooled in the second heat exchanger 40 while maintaining the liquid phase. The liquid heat medium heated by the second heat medium heater 41 is to be discharged from the second heat medium heater 41 by the head pressure of the liquid heat medium transferred from the second heat exchanger 40 to the second heat medium heater 41 . can

At this time, the second heat exchanger 40 is provided on the upper side of the second heat exchanger 41, and only the head pressure of the liquid heat transferred from the second heat exchanger 40 causes the liquid heat discharged from the second heat exchanger 41 to It may not be easy to transfer to the second heat exchanger 40 .

Accordingly, in this embodiment, by providing a heat medium pump 42 on the upper side of the second heat medium heater 41 , the liquid heat medium discharged from the second heat medium heater 41 is pressurized to effectively heat the heat medium with the second heat exchanger 40 . can transmit In addition, since the pressure of the heat medium supplied to the second heat exchanger 40 is controlled by the heat pump 42 , heat exchange between the heat medium and the liquefied gas in the second heat exchanger 40 can be effectively performed.

The heat heater 32 and the second heat heater 41 may be provided in the inner hull of the ship, and the heat pump 42 may be provided in the Bosun Store of the ship, and the heat drum 31 , the heat exchanger 30 , and the second heat exchanger 40 may be provided on the upper deck of the ship. By setting the positions at which the heat exchanger 30, the second heat exchanger 40, the heat drum 31, the heat pump 42, the heat heater 32, and the second heat exchanger 41 are provided as described above, It is possible to further improve the installation utility of the liquefied gas processing system (1) in the ship, and it may be possible to stably drive the liquefied gas processing system (1).

4 is a conceptual diagram of a liquefied gas processing system according to a third embodiment of the present invention.

Referring to FIG. 4 , the liquefied gas processing system 1 according to the third embodiment of the present invention includes a liquefied gas storage tank 10 , a liquefied gas supply line L10 , a first heat exchanger 30 , and a second It includes a heat exchanger 40 , a first heat medium circulation line L20 , and a second heat medium circulation line L30 .

In the gas treatment system 1 according to the third embodiment of the present invention, a plurality of first heat exchangers 30 are provided in parallel on the first heat medium circulation line L20 compared to the first embodiment, and a plurality of second heat exchangers 30 are provided in parallel. 1 heat heater 32 may be provided in parallel.

The liquefied gas supply line (L10) is branched between the boosting pump 21 and the first heat exchanger (30), and the branched liquefied gas supply line (L10') is rejoined in the second heat exchanger 40 downstream. there is. A first heat exchanger 30 may be provided in the liquefied gas supply line L10, and an additional first heat exchanger 30' may be provided in the branched liquefied gas supply line L10'. 4 shows that the two first heat exchangers 30 are provided in parallel, three or more first heat exchangers 30 may be provided in parallel.

A common line (L23) for bringing the first heat medium discharged from each of the plurality of first heat exchangers 30 to be transferred to each of the plurality of first heat exchangers 32 is connected to the first heat exchanger 30 and the first heat medium. It may be provided between the heaters 32 .

The first heat from the first heat exchanger 30 is discharged through the heat recovery line L22, and the first heat from the additional first heat exchanger 30' is discharged through the additional heat recovery line L22'. The point at which the heat recovery line L22 and the additional heat recovery line L22' join may be the starting point of the common line L23.

The common line L23 may be connected to the first heat heater 32 via the heat drum 31 . In this case, the common line L23 may be branched from the upstream of the first heat medium heater 32 , and may be connected to each of the first heat medium heater 32 and the additional first heat medium heater 32 ′.

That is, the first heat medium discharged from each of the plurality of first heat exchangers 30 may be mixed in the common line L23 , and the mixed first heat medium may be transmitted to the plurality of first heat medium heaters 32 , respectively.

4, the first heat medium vaporized in the first heat medium heater 32 is supplied to the additional first heat exchanger 30' through the heat medium supply line L21, and in the additional first heat medium heater 32' Although it is illustrated that the vaporized first heat medium is supplied to the first heat exchanger 30 through the additional heat medium supply line L21', on the contrary, the first heat medium heater 32 and the first heat exchanger 30 are connected and an additional first heat exchanger 32' and an additional first heat exchanger 30' may be connected.

A plurality of second heat exchangers 40 may be provided in parallel in the second heat medium circulation line L30, and a plurality of second heat medium heaters 41 may be provided in parallel.

A second heat exchanger 40 is provided downstream of the first heat exchanger 30 of the liquefied gas supply line L10, and an additional first heat exchanger 30 downstream of the branched liquefied gas supply line L10' An additional second heat exchanger 40' may be provided.

A common line (not shown) that joins the second heat medium discharged from each of the plurality of second heat exchangers 40 and transfers them to each of the plurality of second heat exchangers 41 is formed with the second heat exchanger 40 and It may be provided between the second heat medium heater (41).

The second heat medium discharged from each of the plurality of second heat exchangers 40 may be mixed in a common line, and the mixed second heat medium may be transmitted to each of the plurality of second heat exchangers 41 . The second heat medium heated by the second heat medium heater 41 and the additional second heat medium heater 41 ′ may be merged downstream of the second heat medium heater 41 and transferred to the heat medium pump 42 .

A plurality of heat transfer pumps 42 may be provided in parallel, and the second heat medium may be delivered to each of the plurality of second heat exchangers 40 by pressurizing the second heat medium discharged from the plurality of second heat exchangers 41 . there is.

In this embodiment, by providing a common line between the heat exchanger and the heat medium heater, it is possible to further simplify the heat medium circulation line and reduce the installation man-hours. In addition, since the heat medium discharged from the plurality of heat exchangers is mixed, the heat medium of the same condition is supplied to each heat medium heater, so that it is possible to more easily control the driving conditions of the heat medium heater.

5 is a conceptual diagram of a liquefied gas processing system according to a fourth embodiment of the present invention. Specifically, FIG. 5 is a conceptual diagram at the time of initial operation of the heat exchanger 30 of the liquefied gas processing system 1 according to the fourth embodiment of the present invention. For reference, a valve marked in black in FIG. 5 indicates a closed state.

5, the liquefied gas processing system 1 according to the fourth embodiment of the present invention includes a liquefied gas storage tank 10, a heat medium circulation line L20, a heat medium supply line L21, and a heat recovery line ( L22), a heat exchanger 30, a heat medium heater 32, and a start-up pump (70).

The heat exchanger 30, the heat medium heater 32, the heat medium circulation line (L20), the heat medium supply line (L21), the heat medium recovery line (L22) in the liquefied gas processing system 1 according to the fourth embodiment of the present invention Each of the first heat exchanger 30, the first heat medium heater 32, the first heat medium circulation line (L20), the heat medium supply line (L21) in the liquefied gas processing system 1 according to the first embodiment , may be the same as the heat recovery line L22, respectively. In addition, the gas processing system 1 according to the fourth embodiment of the present invention may further include a startup pump 70 compared to the first embodiment above.

In a conventional heat medium circulation system that heats liquefied gas using the latent heat of a heat medium, seawater is used to vaporize the heat, and the vaporized heat is used to heat the liquefied gas. At this time, it was impossible to vaporize the heat through heat exchange with seawater at the operating pressure of the heat medium circulation system during the initial start-up of the heat exchanger. In order to vaporize the heat by using seawater in the heat exchanger, a separate startup process was required to heat exchange the heat with liquefied gas supplied to the heat exchanger to lower the temperature and saturation pressure of the heat.

However, the pipe connected from the heat heater to the heat exchanger flows through the gas and is larger than the diameter of the pipe through which the liquid flows, and both the liquid pipe and the gas pipe of the heat medium circulation system must be circulated as a liquid heat medium during the startup process. Accordingly, there is a problem in that the amount of heat required in the heat medium circulation system increases, and the volume of the heat medium drum for storing the liquid heat discharged from the heat exchanger must be increased.

On the other hand, in this embodiment, by providing the startup pump 70, the initial driving process of the heat exchanger 30 can be efficiently performed, and this will be described.

The heat exchanger 30 and the heat heater 32 are provided in the heat medium circulation line L20, and the liquid heat discharged from the heat exchanger 30 is temporarily stored in the heat medium drum 31 through the heat recovery line L22. It may be delivered to the fruit heater 32 . The heat transferred to the heat heater 32 may be vaporized through seawater, and the vaporized heat may be delivered to the heat exchanger 30 through the heat medium supply line L21.

A first shutoff valve 33 is provided in the heat medium recovery line L22 to control the flow of liquid heat transferred from the heat exchanger 30 to the heat medium heater 32 , and the heat medium supply line L21 has a second shutoff valve 33 . A valve 34 may be provided to control the flow of gaseous heat transferred from the heat medium heater 32 to the heat exchanger 30 .

At this time, the startup line L24 in which the startup pump 70 is provided is branched between the heat medium drum 31 of the heat medium recovery line L22 and the first shutoff valve 33, It may be connected between the second shut-off valve 34 and the heat exchanger 30 . A third shut-off valve 71a may be provided in the startup line L24 to block the flow of heat transferred from the heat recovery line L22 to the startup pump 70 .

When the heat exchanger 30 is initially operated, the first shut-off valve 33 and the second shut-off valve 34 are sealed so that the liquid heat medium discharged from the heat exchanger 30 bypasses the heat medium heater 32 and starts up. may be introduced into the line L24. At this time, the third shut-off valve 71a is opened, and the liquid heat flowing into the startup line L24 may be pressurized by the startup pump 70 and forcibly supplied to the heat exchanger 30 .

The liquid heat medium pressurized by the startup pump 70 and supplied to the heat exchanger 30 exchanges heat with the low-temperature liquefied gas supplied to the heat exchanger 30, thereby reducing the temperature and saturation pressure of the heat medium. When the temperature and saturation pressure of the heat medium are sufficiently lowered through the startup process, it is possible to vaporize by heat exchange with seawater in the heat medium heater 32 .

That is, by providing the startup line (L24) and the startup pump (70), the process in which the liquid heat medium is supplied to the heat exchanger (30) via the heat medium heater (32) in the startup process of the heat exchanger (30) Since it can be omitted, the amount of heat flowing in the heat medium circulation line L20 can be effectively reduced, the power required for the startup process can be reduced, and the volume of the heat medium drum 31 and the like can be reduced.

In addition, the startup pump 70 is used to forcibly supply liquid heat flowing in the heat recovery line (L22) to the heat medium supply line (L21) during the initial operation of the heat exchanger (30), and the boosting pump (21) ), a heat pump 42, and the like, a smaller pump can be used. In addition, the startup pump 70 may be provided in the ship's boss store (Bosun Store).

The pipe through which the liquid heat of the startup line L24 flows may be a small pipe having a smaller diameter than the pipe through which the heat of the heat recovery line L22 and the heat supply line L21 flows.

The heat drum 31 may be located below the heat exchanger 30 , and the liquid heat discharged from the heat exchanger 30 may be introduced into the heat drum 31 by gravity and the load of the heat medium. The start-up pump 70 may be located below the heat drum 31, and the liquid heat discharged from the heat drum 31 may be transferred to the startup pump 70 by gravity and the load of the heat medium. .

As such, in this embodiment, by providing a separate start-up line L24 and a start-up pump 70 in the heat medium circulation line L20, the start-up process of the heat exchanger 30 can be effectively performed, and the conventional Compared to the fruit circulation system, CAPEX and OPEX can be effectively reduced.

6 is a conceptual diagram of a liquefied gas processing system according to a fifth embodiment of the present invention. Specifically, FIG. 6 is a conceptual diagram during normal operation of the heat exchanger 30 of the liquefied gas processing system 1 according to the fourth embodiment of the present invention. For reference, a valve marked in black in FIG. 6 indicates a closed state.

As described above, when the initial operation of the heat exchanger 30 using the startup pump 70 is completed and the temperature and saturation pressure of the heat medium are sufficiently lowered, the heat is vaporized through heat exchange with seawater in the heat medium heater 32 . become possible Accordingly, normal operation of the heat exchanger 30 may be performed, and the heat medium vaporized in the heat medium heater 32 and the liquefied gas may exchange heat in the heat exchanger 30 .

During normal operation of the heat exchanger 30, the third shut-off valve 71a is closed and the first shut-off valve 33 and the second shut-off valve 34 are opened, and the liquid heat discharged from the heat exchanger 30 is a heat medium. It may be supplied to the heat medium heater 32 via the drum 31 . At this time, a third shut-off valve 71b may be additionally provided downstream of the start-up pump 70 of the start-up line L24, and the additional third shut-off valve 71b is closed to seal the start-up pump 70 ) can be prevented from flowing into the liquid heat exchanger (30) remaining in the heat exchanger (30).

The liquid heat transferred to the heat exchanger 32 may be vaporized by heat exchange with seawater, and the vaporized heat may be supplied to the heat exchanger 30 . At this time, due to the head pressure of the liquid heat discharged from the heat exchanger 30 and delivered to the heat medium heater 32 , the heat vapor vaporized in the heat medium heater 32 is discharged from the heat medium heater 32 to pass the heat supply line L21 . Accordingly, it may be supplied to the heat exchanger 30 .

7 is a conceptual diagram of a liquefied gas processing system according to a sixth embodiment of the present invention.

7, the liquefied gas processing system 1 according to the sixth embodiment of the present invention includes a liquefied gas storage tank 10, a liquefied gas supply line L10, a printed circuit board type heat exchanger 80, It includes a first heat medium circulation line (L20) and a second heat medium circulation line (L30). The gas treatment system 1 according to the sixth embodiment of the present invention is a printed circuit board type heat exchanger ( 80) may be provided.

The printed circuit board type heat exchanger 80 is provided in the liquefied gas supply line L10, and can exchange the liquefied gas with the first heat medium and the second heat medium. That is, the printed circuit board type heat exchanger 80 is at least parallel to the liquefied gas supply line L10 and a flow path (not shown) through which low temperature liquefied gas flows, and the first heat medium circulation line L20 and parallel to the high temperature A flow path through which the first heat medium (not shown) flows, and a flow path (not shown) through which a high temperature second heat flows in parallel with the second heat medium circulation line L30 may be provided.

In the printed circuit board type heat exchanger 80 , the liquefied gas flow may first exchange heat with the first heat medium stream and then heat exchange with the second heat medium flow. In this case, the first heat flow and the second heat flow may be independently provided in the printed circuit board type heat exchanger 80 .

By providing a printed circuit board type heat exchanger 80 in which the first heat exchanger 30 and the second heat exchanger 40 are integrated, the first heat exchanger 30 and the second heat exchanger 40 are separately separated. Compared to the provided system, it is possible to effectively reduce the installation space of the liquefied gas processing system 1 in the ship. In addition, the printed circuit board type heat exchanger 80 is easy to maintain and repair, and since the installation space is reduced, an operator can more easily install, maintain, and repair work.

When the liquefied gas having a pressure less than the critical pressure is supplied to the printed circuit board type heat exchanger 80, the liquefied gas may be vaporized by heat exchange with the first heat flow, and the vaporized liquefied gas may be vaporized by the second heat flow can be heated.

When the liquefied gas having a pressure greater than or equal to the critical pressure is supplied to the printed circuit board type heat exchanger 80, the liquefied gas may be heated by sequentially exchanging heat with the first heat flow and the second heat flow in a supercritical state. At this time, the liquefied gas flow and the first heat flow can exchange heat until a temperature reversal in which the temperature of the liquefied gas is higher than the temperature of the heat medium can occur, and in the section where the temperature reversal can occur, the liquefied gas flow and the second heat flow flow This heat exchange is possible.

The first heat medium circulation line (L20) may include a startup line (L24) and a startup pump (70), and the configuration for initial driving and normal driving of the first heat exchanger (30) is the first embodiment of the present invention. It is the same as that described in Example 4 and Example 5.

8 is a conceptual diagram of a liquefied gas processing system according to a seventh embodiment of the present invention. Specifically, FIG. 8 is a conceptual diagram at the time of initial operation of the first heat exchanger 30 of the liquefied gas processing system 1 according to the seventh embodiment of the present invention. For reference, a valve marked in black in FIG. 8 indicates a closed state.

In the gas processing system 1 according to the seventh embodiment of the present invention, a plurality of first heat exchangers 30 are provided in parallel in the first heat medium circulation line L20 compared to the fourth embodiment, and a plurality of second heat exchangers 30 are provided in parallel. 1 heat heater 32 may be provided in parallel.

A common line (L23) for joining the first heat medium discharged from each of the plurality of first heat exchangers 30 and transferring them to each of the plurality of first heat medium heaters 32 is connected to the first heat exchanger 30 and the first heat medium It may be provided between the heaters (32).

The start-up line L24 is branched between the heat-heat drum 31 and the first shut-off valve 33 of the common line L23, and the second shut-off valve 34 of the heat-heat supply line L21 and an additional first heat exchange It may be connected between the groups 30'. A start-up branch branched from the downstream of the start-up pump 70 of the start-up line L24 and connected between the second shut-off valve 34' of the additional heat supply line L21' and the first heat exchanger 30 A line L25 may be provided.

When the first heat exchanger 30 is initially operated, the first shut-off valve 33 and the second shut-off valves 34 and 34' are closed, so that the first heat medium in the liquid phase discharged from the first heat exchanger 30 is removed. 1 Bypassing the heat medium heater 32, it can be introduced into the startup line (L24). At this time, the third shut-off valve 71a is opened, and the liquid first heat medium flowing into the startup line L24 may be pressurized by the startup pump 70 . A part of the pressurized first heat medium is transferred to the additional first heat exchanger 30' through the heat medium supply line L21, and another part of the first heat medium is transferred to the first heat exchanger through the startup branch line L25. (30) can be passed.

In this embodiment, even when the plurality of first heat exchangers 30 and the plurality of first heat exchangers 32 are provided in parallel by providing the common line L23, each of the plurality of first heat exchangers 30 It is possible to efficiently complete the preparation for initial operation of the plurality of first heat exchangers 30 by performing an integrated startup process without the need to perform a startup process.

9 is a conceptual diagram of a liquefied gas processing system according to an eighth embodiment of the present invention.

Specifically, FIG. 9 is a conceptual diagram during normal operation of the first heat exchanger 30 of the liquefied gas processing system 1 according to the seventh embodiment of the present invention. For reference, a valve marked in black in FIG. 9 indicates a closed state.

When the first heat exchanger 30 is normally operated, the third shutoff valve 71a and the additional third shutoff valve 71b are closed, and the first shutoff valve 33 and the second shutoff valves 34 and 34' are closed. is opened and the liquid heat medium discharged from the plurality of first heat exchangers 30 may be respectively supplied to the plurality of first heat medium heaters 32 along the common line L23.

The first heat medium in the liquid phase received from the common line L23 is vaporized in the first heat medium heater 32 and may be transferred to the additional first heat exchanger 30' along the heat medium supply line L21, The first heat vapor vaporized in the first heat heater 32 ′ may be transferred to the first heat exchanger 30 along the additional heat supply line L21 ′.

10 is a conceptual diagram of a liquefied gas processing system according to a ninth embodiment of the present invention.

The liquefied gas processing system 1 according to the ninth embodiment of the present invention includes a liquefied gas storage tank 10 , a heat exchanger 30 , a heat medium circulation line L20 , a heat medium drum 31 , and a heat medium heater 32 . , a pump 72 , a control unit 90 , and the like.

Hereinafter, the present embodiment will be mainly described on the points that are different from the previous embodiment, and the parts omitted from the description will be replaced with the previous content.

The heat exchanger 30, the heat drum 31, and the heat heater 32 are provided in the heat medium circulation line (L20), and are sequentially located at different heights in the vertical direction, so that the heat medium in the heat medium circulation line (L20) can be circulated smoothly. That is, the heat medium circulation line (L20) may supply the heat medium discharged from the heat exchanger (30) to the heat medium heater (32), heat it, and then supply it back to the heat exchanger (30).

The heat medium circulation line (L20) is a heat medium supply line (L21) for supplying vapor phase heat to the heat exchanger (30), a heat medium recovery line (L22) and a heat medium heater for receiving liquid heat discharged after being liquefied in the heat exchanger (30). It is provided to connect the upstream and downstream of (32), and may include a startup line (L24) for flowing the heat to the heat medium supply line (L21) during the initial operation of the heat exchanger (30).

The heat exchanger 30 may receive vapor-phase heat-exchange with the liquefied gas, and then discharge the cooled liquid-phase heat-exchange with the liquefied gas. The heat drum 31 may be provided on the heat recovery line L22. The heat drum 31 is provided below the heat exchanger 30 , and the liquid heat discharged from the heat exchanger 30 may be introduced into the heat drum 31 by gravity and the load of the heat medium.

The heat medium drum 31 may temporarily store the liquid heat discharged from the heat exchanger 30 and deliver the liquid heat to the heat medium heater 32 . At this time, the heat medium heater 32 is provided below the heat medium drum 31 , and the liquid heat discharged from the heat medium drum 31 may be transferred to the heat medium heater 32 by gravity and the load of the heat medium. In addition, a pump 72, which will be described later, is provided below the heat medium drum 31, and after the liquid heat medium discharged from the heat medium drum 31 passes through the pump 70 by gravity and the heat of the heat medium, the heat medium heater 32 can be transmitted to

The heat medium heater 32 may vaporize the liquid heat received from the heat medium drum 31 using seawater. The heat medium heater 32 may receive the fruit through the heat medium recovery line L22, heat the fruit, and then transfer it to the heat medium supply line L21. At this time, the liquefied gas vaporized in the heat medium heater 32 is discharged from the heat medium heater 32 by the head pressure of the liquid heat transferred from the heat medium drum 31 or the pump 72 to the heat medium heater 32 , The gaseous heat discharged from the heater 32 may be supplied to the heat exchanger 30 .

The startup line (L24) is branched between the heat medium drum 31 and the heat medium heater 32 of the heat medium recovery line (L22), between the heat medium heater 32 and the heat exchanger 30 of the heat medium supply line (L21) can be connected That is, the startup line L24 may be provided to connect the upstream and downstream of the heat medium heater 32 . The startup line L24 delivers the heat so that the heat can flow to the heat supply line L21 during the initial operation of the heat exchanger 30 . A three-way valve is provided at the point where the start-up line L24 joins the heat medium supply line L21 so that the opening degree can be adjusted according to the operating conditions of the heat exchanger 30 .

The liquefied gas processing system according to this embodiment may include a pump 72 on the heat medium recovery line L22. The pump 72 may be provided at a position lower than the heat exchanger 30 and the heat medium drum 31 along the vertical direction, and may be provided at a location higher than the heat medium heater 32 and the start-up line L24. That is, the pump 72 may be provided upstream of a point at which the startup line L24 branches from the heat medium recovery line L22.

Unlike the startup pump 70 of the previous embodiment, the pump 72 is provided on the heat recovery line L22, but serves to boost the startup of the system and heat heat circulation through the heat medium circulation line L20. can

The pump 72 may forcibly supply heat to the startup line L24 when the heat exchanger 30 is initially operated. In this case, the first shutoff valve 33 and the second shutoff valve 34 respectively provided upstream and downstream of the heat medium heater 32 can block the flow of heat, and are provided on the startup line L24. The heat of the startup line L24 may be delivered to the heat supply line L21 through the three-way valve.

When the heat exchanger 30 starts to operate normally, the liquid heat medium discharged from the heat exchanger 30 circulates through the head pressure, so that the pump 72 may not be operated. In this case, the heat flow is blocked by controlling the fourth shutoff valve 73 and the fifth shutoff valve 72 provided upstream and downstream of the pump 72, respectively, or a bypass provided in the heat recovery line L22. The fruit may be circulated through line L26. The bypass line L26 may be provided to connect the upstream and downstream of the pump 72 . For example, the bypass line L26 branches at a position lower than the heat medium drum 31 in the vertical direction, and rejoins the heat medium recovery line L22 at a position higher than the position where the start-up line L24 branches off. can do.

The pump 72 may forcibly supply the heat medium to the heat medium circulation line L20 when the heat exchanger 30 breaks down or the head pressure of the liquid heat medium discharged from the heat exchanger 30 decreases below a predetermined value. . Liquid heat discharged from the heat exchanger 30 due to an unexpected trip or failure of the heat exchanger 30 itself due to a sudden change in the flow rate of the liquefied gas supplied from the liquefied gas treatment system to the heat exchanger 30 If the head pressure of the circulator is lowered, the circulation of the fruit through the fruit circulation line L20 may be slowed or stopped. In this case, the pump 72 pressurizes the heat medium flowing through the heat medium recovery line L22 to forcibly circulate through the heat medium circulation line L20, so that it can respond to a system failure or a temporary sudden change.

The liquefied gas treatment system may further include an additional heat exchanger and a heating medium heater. Referring to FIG. 10 , the liquefied gas processing system may further include a second heat exchanger 40 and a second heat medium heater 41 for heating the liquefied gas heat-exchanged in the heat exchanger 30 .

The second heat exchanger 40 may heat the liquefied gas using the same heat medium as in the heat exchanger 30 . In this case, the heat medium circulation line (L20) is a heat medium supply line (L21') for supplying the gaseous heat to the second heat exchanger (40), the heat medium receiving the liquid heat discharged after being liquefied in the second heat exchanger (40). A startup line that is provided to connect the upstream and downstream of the recovery line (L22') and the second heat medium heater (41), and flows heat to the heat medium supply line (L21') when the second heat exchanger 40 is initially operated (L24) may be further included.

The heat recovery line L22 for delivering the liquid heat discharged from the heat exchanger 30 and the heat recovery line L22 ′ for delivering the liquid heat discharged from the second heat exchanger 40 are connected to the heat drum 31 . can pass The heat medium discharged from the heat medium drum 31 may flow through the heat medium recovery line L22 through the above-described bypass line L26 or the pump 72 , and a part thereof is branched to the second heat medium heater 41 . can be supplied. The start-up line L24' may branch out from the line supplied to the second heat medium heater 41 and connect the upstream and downstream of the second heat medium heater 41, but is not limited thereto. The start-up line (L24') may be branched out from a lower position than the pump 72 in the vertical direction from the heat recovery line (L22), and the line branched again from the start-up line (L24') is the second heat source It may be connected to a heater 41 .

The liquid heat medium discharged from the second heat exchanger 40 may also be transferred to the second heat medium heater 41 by gravity and the load of the heat medium. The second heat medium heater 41 may maintain the liquid phase or vaporize the liquid heat medium cooled in the second heat exchanger 40 by using seawater. The heat medium heated by the second heat medium heater 41 may be discharged from the second heat medium heater 41 by the head pressure of the liquid heat medium transferred from the second heat exchanger 40 to the second heat medium heater 41 . .

Even when the second heat exchanger 40 and the second heat medium heater 41 are provided, the startup process using the startup line L24 ′ and the pump 72 may be equally applied, and the second heat exchanger 40 ) failure or when the head pressure of the liquid heat medium discharged from the second heat exchanger 40 decreases to a predetermined value or less, the heat medium may be forcibly circulated using the pump 72 .

Although not shown, the liquefied gas processing system according to this embodiment may include a plurality of heat exchangers and a plurality of heat medium heaters, respectively. As shown in FIG. 10, a plurality of heat exchangers may be provided to pass in series based on the flow of liquefied gas, and as shown in FIGS. 8 and 9, a plurality of heat exchangers are installed in parallel based on the flow of liquefied gas You can also prepare a catalog. In each case, the plurality of heat exchangers may use the same heat medium, and natural circulation through the head pressure of the heat medium passing through each heat exchanger and forced circulation using the pump 72 in case of failure are possible.

The liquefied gas processing system may further include a control unit 90 for determining whether to operate the pump 72 . The head pressure of the liquid heat medium discharged from the heat exchanger 30 is directly related to whether the heat medium can be circulated through the heat medium circulation line L20. When the heat medium circulation line L20 includes the heat medium drum 31 , the water level of the liquid heat temporarily stored in the heat medium drum 31 will affect the head pressure of the liquid heat discharged from the heat medium drum 31 . can Accordingly, the present embodiment may further include a control unit 90 for controlling the pump 72 according to the water level of the heat medium drum 31 to maintain a head pressure suitable for heat medium circulation.

Although not shown, the control unit 90 controls the operation of the pump 72 based on a water level sensor for measuring the water level of the liquid heat medium stored in the heat medium drum 31 and the information received from the sensor VFD (variable frequency) drive) may be included. The controller 90 may measure the water level of the heat-heat drum 31 through a water level sensor provided inside or outside the heat-heat drum 31 and control the water level within a range capable of maintaining a desired head pressure.

The control unit 90 includes a pump 72 , a fourth shutoff valve 73 and a fifth shutoff valve 74 provided upstream and downstream of the pump 72 , respectively, and a bypass line L26 that bypasses the pump 72 . ), by adjusting at least one of the sixth shut-off valves 75 provided on the top, it is possible to control the water level of the heat medium drum 31 and the head pressure of the heat medium circulating through the heat medium circulation line L20. That is, the control unit 90 controls the pump 72 and the like so that the water level of the heat medium stored in the heat medium drum 31 can provide more than the head pressure required for circulation of the liquid heat medium based on the normal operation of the heat exchanger 30 . can be controlled

For example, when the water level of the liquid heat medium stored in the heat medium drum 31 is low and the head pressure is insufficient, the controller 90 operates the pump 72 to boost the heat medium to achieve circulation of the heat medium.

For example, when the water level of the liquid heat medium stored in the heat medium drum 31 is high and the head pressure is sufficient, the control unit 90 does not operate the pump 72 and flows the heat through the bypass line L26 without operating the pump 72 . cycle can be achieved.

The control unit 90 continuously considers the operation mode and normal operation of the heat exchangers 30 and 40 to determine the water level of the heat medium stored in the heat medium drum 31 or the head pressure of the liquid heat discharged from the heat medium drum 31 . It can be controlled to ensure the stability of the entire system.

As described above, in this embodiment, in a liquefied gas processing system that provides smooth circulation using the head pressure of the heat exchanger, the heat exchanger can be circulated even when the heat exchanger fails or the head pressure is not sufficiently ensured, so that the system stability can be ensured.

11 is a conceptual diagram of a liquefied gas processing system according to a tenth embodiment of the present invention.

Referring to FIG. 11 , the liquefied gas treatment system 1 according to the tenth embodiment of the present invention includes a liquefied gas storage tank 10 , a heat exchanger 30 , a heat medium circulation line L20 , and a heat medium drum 31 . , including a heat medium heater 32 , a pump 72 , and the like.

Hereinafter, the present embodiment will be mainly described on the points that are different from the previous ninth embodiment, and the parts omitted from the description will be replaced with the previous content.

The liquefied gas processing system according to this embodiment includes a plurality of pumps 72 and 72'. The plurality of pumps 72 and 72 ′ may be provided in parallel on the heat recovery line L22 , and may be disposed under the heat medium drum 31 in the vertical direction.

The plurality of pumps 72 and 72' may have the same processing capacity, but those having different capacities may be arranged in parallel. For example, any one pump 72 may have a capacity of 90% compared to the pump 72 of the ninth embodiment, and the other pump 72' is 10 compared to the pump 72 of the ninth embodiment. % of the capacity. In this case, when the heat exchanger 30 is initially operated, a start-up can be implemented through the pump 72 ′ having a relatively low capacity to supply heat using the startup line L24, and the heat exchanger 30 malfunctions. Alternatively, when the head pressure of the liquid heat medium discharged from the heat exchanger 30 decreases below a predetermined value, forced circulation of the heat medium through the pump 72 having a relatively high capacity may be implemented. A specific one of the plurality of pumps 72 and 72' is not limited to start-up or forced circulation of the medium.

A fourth shut-off valve 73, 73' and a fifth shut-off valve 74, 74' may be provided upstream and downstream of the plurality of pumps 72 and 72', respectively, and although not shown, according to the present embodiment It will be understood that the liquefied gas processing system may also include a control unit to implement a start-up or forced circulation of the heat medium through the control of the valve.

A bypass line L26 may be provided in the heat medium recovery line L22, and the bypass line L26 may be provided to connect upstream and downstream of the pumps 72 and 72'. According to the head pressure of the liquid heat discharged from the heat medium drum 31, heat is supplied to one or more of the bypass line L26 and the plurality of pumps 72 and 72' to maintain the optimum head pressure for heat medium circulation. be able to

As described above, in this embodiment, in a liquefied gas processing system that provides smooth circulation using the head pressure of the heat medium, a plurality of pumps for system startup or forced circulation of the heat medium are provided to maintain the optimum head pressure. Thus, it is possible to secure the stability of the system and provide an energy saving effect.

It goes without saying that the present invention is not limited to the embodiments described above, and a combination of the embodiments or a combination of at least one of the embodiments and a known technology may be included as another embodiment.

Although the present invention has been described in detail through specific examples, this is for the purpose of describing the present invention in detail, and the present invention is not limited thereto. It will be clear that the transformation or improvement is possible.

All simple modifications and variations of the present invention fall within the scope of the present invention, and the specific scope of protection of the present invention will be clarified by the appended claims.

1: Liquefied gas processing system
10: liquefied gas storage tank 11: pump
20: buffer tank 21: boosting pump
30, 30': first heat exchanger 31: heat drum
32, 32': first heat heater 33: first shut-off valve
34, 34': second shut-off valve 40, 40': second heat exchanger
41, 41': second heat heater 42: heat pump
50: expansion drum 60: fruit storage tank
61: heat transfer pump 70: startup pump
71a, 71b: third shut-off valve 72, 72': pump
73, 73': fourth shut-off valve 74, 74': fifth shut-off valve
75: sixth shut-off valve
80: printed circuit board type heat exchanger 90: control unit
100: demand
L10, L10': liquefied gas supply line L20: first heat medium circulation line
L21, L21': Fruit supply line L22, L22': Fruit recovery line
L23: Common line L24, L24': Startup line
L25: Startup branch line L26: Bypass line
L30: second heat medium circulation line L50: pressure compensation line
L60: Fruit transfer line

Claims (9)

a heat exchanger for heating the liquefied gas supplied from the liquefied gas storage tank using the latent heat of the heat medium; and
and a heat medium circulation line that heats the heat medium discharged from the heat exchanger and circulates it to the heat exchanger,
The fruit circulation line is
a heat supply line for supplying gaseous heat to the heat exchanger;
a heat recovery line for receiving the liquid heat liquefied and discharged from the heat exchanger;
a heat heater provided between the heat medium supply line and the heat medium recovery line to vaporize the liquid heat;
a start-up line provided to connect the upstream and downstream of the heat exchanger, and for flowing the heat to the heat supply line when the heat exchanger is initially operated; and
A pump is provided upstream of the branching point of the startup line in the heat recovery line and forcibly supplies heat to the startup line when the heat exchanger is initially operated,
The liquefied gas treatment system, characterized in that the heat exchanger is circulated by the head pressure of the liquid heat discharged from the heat exchanger during normal operation of the heat exchanger. The method of claim 1,
When the heat exchanger is normally operated, the gaseous heat from the heat supply line is supplied to the heat exchanger by the pressure of the liquid heat flowing in the heat recovery line. The method of claim 1,
The pump is
The liquefied gas treatment system, characterized in that when the heat exchanger malfunctions or the head pressure of the liquid heat medium discharged from the heat exchanger decreases below a predetermined value, the heat medium is forcibly supplied to the heat medium circulation line. The method of claim 1,
The pump is
A liquefied gas processing system, characterized in that provided in parallel in a plurality on the heat medium recovery line. 5. The method of claim 4,
The plurality of pumps,
Liquefied gas processing system, characterized in that it has different capacities. The method of claim 1,
Further comprising a control unit for determining whether to operate the pump,
The fruit circulation line is
It is provided at a higher position than the pump along the vertical direction, further comprising a heat drum for storing the heat discharged from the heat exchanger,
The control unit is
Liquefied gas processing system, characterized in that for controlling the pump according to the water level of the heat medium stored in the heat drum drum. 7. The method of claim 6,
The control unit is
The liquefied gas treatment system, characterized in that the pump is controlled so that the water level of the heat medium stored in the heat medium drum provides more than the head pressure required for circulation of the liquid heat medium during normal operation of the heat exchanger. The method of claim 1,
The fruit circulation line is
Liquefied gas processing system, characterized in that it further comprises a bypass line bypassing the pump. The method of claim 1,
The fruit circulation line is
A plurality of the heat exchanger is provided in parallel, a plurality of the heat medium heater is provided in parallel,
A liquefied gas processing system, characterized in that the heat discharged from each of the plurality of heat exchangers is merged and delivered to each of the plurality of heat exchangers.

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