KR101934816B1 - Gas Treatment System and Vessel having same - Google Patents

Abstract

A gas processing system according to an embodiment of the present invention includes a plurality of evaporation gas compressors provided in parallel to each other to pressurize the evaporation gas generated from the liquefied gas storage tank and supply the same to a customer; And a control unit for controlling the evaporative gas compressor according to an amount of evaporative gas generated in the liquefied gas storage tank, wherein the control unit controls at least one of the plurality of evaporative gas compressors in a standby state And the evaporative gas compressors which are in the standby state in the standby control before and after the normal control are different from each other.

Description

TECHNICAL FIELD [0001] The present invention relates to a gas treatment system and a vessel including the same,

The present invention relates to a gas treatment system and a vessel including the same.

Liquefied natural gas (Liquefied natural gas), Liquefied petroleum gas (Liquefied petroleum gas) and other liquefied gas are widely used in place of gasoline or diesel in recent technology development.

Liquefied natural gas is a liquefied natural gas obtained by refining natural gas collected from a gas field. It is a colorless and transparent liquid with almost no pollutants and high calorific value. It is an excellent fuel. On the other hand, liquefied petroleum gas is a liquid fuel made by compressing gas containing propane (C3H8) and butane (C4H10), which come from oil in oil field, at room temperature. Liquefied petroleum gas, like liquefied natural gas, is colorless and odorless and is widely used as fuel for household, business, industrial, and automotive use.

Such liquefied gas is stored in a liquefied gas storage tank installed on the ground or stored in a liquefied gas storage tank provided in a ship which is a means of transporting the ocean. The liquefied natural gas is liquefied to a volume of 1/600 The liquefaction of liquefied petroleum gas has the advantage of reducing the volume of propane to 1/260 and the content of butane to 1/230, resulting in high storage efficiency. The temperature and pressure necessary for driving the engine using such liquefied gas as fuel may be different from the state of the liquefied gas stored in the tank.

In addition, when LNG is stored in a liquid state, some LNG is vaporized and boil off gas (BOG) is generated as heat penetration occurs in the tank. Such evaporation gas may cause problems in a liquefied gas processing system. In order to solve the problem by discharging the evaporation gas to the outside (in the past, the evaporation gas was simply discharged to the outside in order to lower the tank pressure by lowering the tank pressure), the problem was solved. However, .

 In recent years, researches and developments have been actively conducted on utilization methods such as recycling the generated evaporated gas through a liquefied gas, liquefying it, and supplying it to the engine as a technique for efficiently processing the evaporated gas.

It is an object of the present invention to provide a gas processing system for effectively supplying liquefied gas and / or evaporative gas from a liquefied gas storage tank to a customer, and a vessel containing the same, and / Or a vessel having an arrangement optimized in the ship, and a vessel including the same.

The gas processing system according to the present invention comprises: a plurality of evaporation gas compressors provided in parallel to each other, the evaporation gas compressors being provided in a liquefied gas storage tank to pressurize and supply the evaporated gas to a customer; And a control unit for controlling the evaporative gas compressor according to an amount of evaporative gas generated in the liquefied gas storage tank, wherein the control unit controls at least one of the plurality of evaporative gas compressors in a standby state And the evaporative gas compressors which are in the standby state in the standby control before and after the normal control are different from each other.

Specifically, the control unit may control at least one of the plurality of evaporative gas compressors to be in the standby state when the evaporative gas generation amount is equal to or less than the preset generation amount, and when the evaporative gas generation amount is again equal to or less than the predetermined generation amount, The remaining one of the evaporation gas compressors can be controlled to the standby state.

Specifically, the evaporative gas compressor includes a constituent compressor in which four or five stages of pistons are connected in series, and four constituent compressors may be provided and connected to each other in parallel.

The controller may further include an evaporation gas generation amount measuring sensor for measuring an evaporation gas generation amount generated in the liquefied gas storage tank, wherein the controller receives the evaporation gas generation amount measured from the evaporation gas generation amount measurement sensor, The driving of the gas compressor can be controlled.

Specifically, the control unit may control one of the evaporative gas compressors to be in the standby state when the evaporative gas generation amount received from the evaporative gas generation amount measurement sensor is equal to or less than the predetermined generation amount, And when the evaporation gas generation amount is again less than the predetermined generation amount, any one of the remainder of the evaporative gas compressor in which the load is increased can be controlled to the standby state.

Specifically, an evaporation gas heat exchanger for exchanging heat between the evaporation gas supplied from the liquefied gas storage tank and the evaporation gas compressed by the evaporation gas compressor; And a bypass line for bypassing the evaporation gas heat exchanger, wherein the control unit controls the evaporation gas supplied from the liquefied gas storage tank to flow through the bypass line when the evaporation gas generation amount is equal to or less than the pre- The evaporation gas heat exchanger is controlled to be supplied to the evaporation gas compressor by bypassing the evaporation gas heat exchanger, wherein when the evaporation gas generation amount exceeds the preset generation amount, evaporation gas supplied from the liquefied gas storage tank is evaporated through the evaporation gas heat exchanger It is possible to partially re-liquefy the evaporated gas compressed in the gas compressor.

Specifically, the predetermined generation amount is an amount of evaporation gas flowing into the evaporation gas compressor at an inefficient point of the evaporation gas compressor, and an inefficiency point of the evaporation gas compressor is a ratio of a flow rate of the evaporation gas compressor to a flow rate of power consumption, And may be a point where power consumption is not reduced even if the flow rate supplied to the evaporative gas compressor is reduced.

Specifically, the load at the inefficient point of the evaporative gas compressor may be 20 to 40% of the flow rate at which the evaporative gas compressor has the maximum load.

Specifically, an evaporative gas decompressor for decompressing heat-exchanged evaporative gas supplied from the evaporative gas heat exchanger; And a gas-liquid separator which receives the decompressed gas from the evaporation gas decompressor and separates the gas and liquid into a liquid phase and a gaseous phase.

Specifically, the customer is a high-pressure consumer that consumes high-pressure evaporation gas at 150 to 350 bar; And a low pressure consumer consuming low pressure vapor of 4 to 8 bar.

Specifically, the evaporation gas supply line connecting the liquefied gas storage tank and the high-pressure consumer, and including the evaporative gas compressor; An evaporation gas branch line branched at the intermediate stage of the evaporation gas compressor on the evaporation gas supply line and connecting the low-pressure consumer; An evaporation gas first return line branched from the evaporation gas supply line downstream of the evaporation gas compressor and connecting the evaporation gas heat exchanger; An evaporation gas second return line connecting the evaporation gas heat exchanger and the gas-liquid separator, the evaporation gas second return line including the evaporation gas decompressor; A flash gas supply line connecting the gas-liquid separator and the evaporation gas heat exchanger upstream on the evaporation gas supply line; And a re-liquefied gas return line connecting the gas-liquid separator and the liquefied gas storage tank.

Specifically, the evaporation gas generation amount measuring sensor can calculate the evaporation gas generation amount through the internal pressure of the liquefied gas storage tank.

Specifically, the evaporative gas compressor may be a standard high pressure compressor.

Specifically, it may be a vessel characterized by including the gas treatment system.

The gas treatment system and the vessel including the same according to the present invention have the effect of effectively supplying the liquefied gas and / or the evaporated gas from the liquefied gas storage tank to the customer to enhance the stability and reliability of the system, So that the space utilization on the ship is improved.

1 is a conceptual diagram of a gas processing system according to an embodiment of the present invention.
2 is a conceptual diagram of a gas processing system according to another embodiment of the present invention.
3 is a conceptual diagram of a gas processing system according to another embodiment of the present invention.
4 is a graph illustrating power consumption versus flow rate of an evaporative gas compressor according to an embodiment of the present invention.
5 is a graph showing the amount of evaporative gas generated in the liquefied gas storage tank versus the operating time of the ship according to the embodiment of the present invention.
6 is a side view of a vessel having a gas treatment system according to an embodiment of the present invention.
7 is an interior plan view of a cargo compartment of a ship in accordance with an embodiment of the present invention.
8 is an internal plan view of a cargo compartment of a ship according to another embodiment of the present invention.
9 is an internal sectional view of a cargo compressor room of a ship according to another embodiment of the present invention.
10 is a modified internal sectional view of a cargo compartment of a ship according to another embodiment of the present invention.

BRIEF DESCRIPTION OF THE DRAWINGS The objects, particular advantages and novel features of the present invention will become more apparent from the following detailed description taken in conjunction with the accompanying drawings, in which: FIG. It should be noted that, in the present specification, the reference numerals are added to the constituent elements of the drawings, and the same constituent elements are assigned the same number as much as possible even if they are displayed on different drawings. In the following description, well-known functions or constructions are not described in detail since they would obscure the invention in unnecessary detail.

Hereinafter, the liquefied gas may be LPG, LNG, or ethane, and may be, for example, LNG (Liquefied Natural Gas), and the evaporation gas may refer to BOG (Boil Off Gas) such as natural vaporized LNG.

The liquefied gas can be referred to irrespective of the state change, such as liquid state, gas state, mixed state of liquid and gas, supercooled state, supercritical state, and the like. Further, it is apparent that the present invention is not limited to the liquefied gas to be treated, but may be a liquefied gas processing system and / or an evaporative gas processing system, and the systems of the following drawings may be applied to each other. In addition, the mixed fluid described below may be a mixed vaporized gas or a fluid containing at least a part of the liquid phase.

Further, the embodiments of the gas treatment system 2 of the present invention may be configured in combination with each other, and the addition of the respective structures may be made to be an intersection with each other. The gas treatment system 2 according to an embodiment of the present invention may be mounted on the hull H and the vessel 1 may be a ship such as an LNG carrier, a container carrier, or the like, but is not limited thereto.

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

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

1, a gas processing system 2 according to an embodiment of the present invention includes a liquefied gas storage tank 10, an evaporation gas heat exchanger 20, an evaporation gas decompressor 30, a gas- The first demand site 71, the second demand site 72, the first control unit 90, and the second control unit 91. The first to fourth evaporative gas compressors 51 to 54, the first demand site 71, the second demand site 72,

Hereinafter, a gas processing system 2 according to an embodiment of the present invention will be described with reference to FIG.

Prior to describing the individual configurations of the gas processing system 2 according to the embodiment of the present invention, the basic flow paths for organically connecting the individual structures will be described. Here, the passage is a passage through which the fluid flows, and may be a line. However, the present invention is not limited thereto.

In the embodiment of the present invention, the evaporation gas supply line L1, the evaporation gas first return line L2, and the evaporation gas branch line L3. The second gas return line L4, the re-liquefaction return line L5, the flash gas supply line L6, and the evaporation gas bypass line L7. Valves (not shown) capable of adjusting the opening degree may be provided in each line, and the supply amount of the evaporation gas may be controlled according to the opening degree of each valve.

The evaporation gas supply line L1 connects the liquefied gas storage tank 10 and the first customer 71 and includes the evaporation gas heat exchanger 20 and the first to fourth evaporative gas compressors 51 to 54 So that the evaporated gas generated in the liquefied gas storage tank 10 can be supplied to the first consumer 71. At this time, the evaporation gas supply line L1 may connect the first to fourth evaporative gas compressors 51 to 54 in parallel.

The evaporation gas supply line L1 may include an evaporation gas first flow valve 81a upstream of the evaporation gas heat exchanger 20 and may be connected to the evaporation gas heat exchanger 20 via an evaporation gas first flow valve 81a, It is possible to control the flow rate of the evaporation gas supplied to the unit 20. Here, the evaporation gas first flow valve 81a may be connected to the first control unit 90 in a wired or wireless manner to receive the opening control command of the first control unit 90. [

The first return line L2 of the evaporation gas is branched from the rear end of the first to fourth evaporative gas compressors 51 to 54 on the evaporation gas supply line L1 and is connected to the evaporation gas heat exchanger 20, To the evaporation gas heat exchanger (20) at least a part of the evaporation gas compressed in the first to fourth evaporation gas compressors (51 to 54).

The evaporation gas branch line (L3) The refrigerant can be branched at the middle end of the first to fourth evaporative gas compressors 51 to 54 on the evaporative gas supply line L1 and connected to the second consumer 72. The first to fourth evaporative gas compressors 51 to 54 ) To the second customer site 72. The second customer site 72 can be operated by the user. Here, the evaporation gas branch line L3 is shown as branched between the first stage and the second stage of the fourth evaporative gas compressor 54, but the present invention is not limited thereto and the first to third evaporative gas compressors 51 to 53 May be branched between each of the first and second stages. Whereby the evaporation gas branch line L3 can supply the evaporated gas compressed at a pressure of 2 to 6 bar to the second customer.

The second return line L4 of the evaporation gas is connected to the evaporation gas heat exchanger 20 and the gas-liquid separator 40 and is provided with an evaporation gas decompressor 30 so that the evaporation gas heat exchanged in the evaporation gas heat exchanger 20 To the gas-liquid separator (40) by depressurizing the gas-liquid separator (30).

The re-liquefaction return line L5 connects the gas-liquid separator 40 and the liquefied gas storage tank 10 and can supply the liquid phase separated from the gas-liquid separator 40 to the liquefied gas storage tank 10.

The flash gas supply line L6 can be connected upstream of the gas-liquid separator 40 and the evaporation gas heat exchanger 20 on the evaporation gas supply line L1, and the gas phase separated from the gas- Can be joined to the line L1.

The evaporation gas bypass line L7 branches off upstream of the evaporation gas heat exchanger 20 on the evaporation gas supply line L1 and is connected downstream of the evaporation gas heat exchanger 20 on the evaporation gas supply line L1, The second gas flow rate valve 81b is provided to bypass the evaporation gas heat exchanger 20 to supply the evaporated gas supplied from the liquefied gas storage tank 10 to the first to fourth evaporative gas compressors 51 to 54 . Here, the evaporation gas second flow valve 81b may be connected to the first control unit 90 in a wired or wireless manner to receive the opening control command of the first control unit 90. [

Hereinafter, individual constitutions which are organically formed by the above-described respective lines (L1 to L7) to implement the gas processing system 2 will be described.

The liquefied gas storage tank 10 stores the liquefied gas to be supplied to the first and second consumers 71 and 72. The liquefied gas storage tank 10 must store the liquefied gas in a liquid state, in which case the liquefied gas storage tank 10 may have the form of a pressure tank.

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

The evaporation gas heat exchanger 20 is provided between the liquefied gas storage tank 10 and the first to fourth evaporative gas compressors 51 to 54 on the evaporation gas supply line L1 and is provided in the liquefied gas storage tank 10 It is possible to exchange heat between the supplied evaporation gas and the evaporated gas compressed by the first to fourth evaporative gas compressors 51 to 54.

The evaporated gas compressed in the first to fourth evaporative gas compressors 51 to 54 among the evaporated gases heat-exchanged in the evaporative gas heat exchanger 20 is supplied to the evaporative gas decompressor 30 and the evaporated gas heat exchanger 20 The evaporated gas supplied from the liquefied gas storage tank 10 among the evaporated gases heat-exchanged in the first to fourth evaporative gas compressors 51 to 54 may be supplied to the first to fourth evaporative gas compressors 51 to 54.

Accordingly, the evaporated gas compressed by the first to fourth evaporative gas compressors 51 to 54 can be partially re-liquefied by receiving the cold heat from the evaporated gas supplied from the liquefied gas storage tank 10, The evaporation gas supplied from the first to fourth evaporative gas compressors 51 to 54 is supplied with the heat source from the evaporated gas compressed by the first to fourth evaporative gas compressors 51 to 54 and supplied to the first to fourth evaporative gas compressors 51 to 54, .

The evaporation gas decompressor 30 is pressurized by the first to fourth evaporative gas compressors 51 to 54 to decompress or expand the evaporated gas heat exchanged in the evaporation gas heat exchanger 20 to liquefy at least a part thereof. For example, the evaporation gas decompressor 30 may reduce the evaporation gas of 150 to 350 bar to 1 to 10 bar, and the evaporation gas may be liquefied and reduced to 1 bar when transferred to the liquefied gas storage tank 10, The evaporation gas can be cooled during decompression.

In this embodiment, the evaporated gas pressurized by the first to fourth evaporative gas compressors 51 to 54 is heat-exchanged with the evaporated gas supplied from the liquefied gas storage tank 10 in the evaporative gas heat exchanger 20, The pressure can maintain the discharge pressure discharged from the first to fourth evaporative gas compressors 51 to 54.

Accordingly, in the present embodiment, it is possible to utilize that the evaporated gas pressurized by the first to fourth evaporative gas compressors 51 to 54 is maintained at a high pressure even after heat exchange in the evaporative gas heat exchanger 20, So that the evaporation gas is decompressed through the evaporation gas decompressor 30 so that the evaporation gas is further cooled. Accordingly, the evaporated gas pressurized in the first to fourth evaporative gas compressors 51 to 54 is partially re-liquefied in the evaporative gas heat exchanger 20, but finally can be completely liquefied in the evaporative gas decompressor 30.

Specifically, the evaporation gas may be multi-stage pressurized by the first to fourth evaporative gas compressors 51 to 54 to have a pressure of 150 to 350 bar, and the temperature may be around 45 degrees. The evaporated gas raised to a temperature of about 45 degrees is recovered by the evaporation gas heat exchanger 20 and is heat-exchanged with the evaporation gas of about 100 degrees supplied from the liquefied gas storage tank 10 and cooled to a temperature of about -97 degrees And then supplied to the evaporative gas decompressor 30. At this time, the evaporation gas in the evaporation gas decompressor 30 is cooled by the reduced pressure and can have a pressure of about 1 bar and a temperature of about -162.3 degrees.

As described above, in this embodiment, since the evaporation gas has a temperature lower than -162 deg. C due to the decompression of the evaporation gas through the evaporation gas decompressor 30, the evaporation gas liquefaction rate of about 30-40% can be realized. This is because the larger the pressure range in which the evaporation gas is decompressed, the greater the cooling effect of the evaporation gas can be.

Here, the evaporation gas decompressor 30 may be a Joule-Thomson valve. Alternatively, the evaporative gas decompressor 30 may be formed of an expander (expander).

The inflator can be driven without using any additional power. Particularly, by utilizing the generated power as electric power for driving the first to fourth evaporative gas compressors 51 to 54, the efficiency of the gas processing system 2 can be improved. The power transmission may be accomplished by, for example, a gear connection or an electric conversion and the like.

A gas-liquid separator (40) temporarily stores evaporated or decompressed gas in the evaporative gas decompressor (30), and separates the evaporated gas into liquid and gas through gravity.

At this time, the gas is flash gas, and the temperature is approximately -162.3 degrees. The flash gas and the -100 degree evaporation gas generated in the liquefied gas storage tank 10 are mixed in the upstream of the evaporation gas heat exchanger 20 to become a mixed gas having a temperature of -110 to -120 degrees (about-114 degrees) , And the mixed gas may be introduced into the evaporation gas heat exchanger 20 at a temperature of -110 to -120 degrees (-114 degrees).

Thus, the 45-degree evaporation gas recovered along the first return line L2 of the evaporation gas is supplied to the evaporation gas heat exchanger 20 through the evaporation gas supply line L1, . It can be seen that additional cooling of the evaporated gas can be realized when there is no flash gas recovery (45 degrees of evaporation gas versus -100 degrees of evaporation and heat exchange).

Therefore, the evaporated gas discharged from the evaporated gas heat exchanger 20 and flowing into the evaporated gas decompressor 30 may be about -112 degrees lower than the case where no flash gas circulates (about -97 degrees), and the evaporated gas When the pressure is reduced by the pressure reducer 30, it can be cooled to about -163.7 degrees. In this case, more evaporative gas can be liquefied by the evaporative gas decompressor 30 and recovered to the liquefied gas storage tank 10 than when the flash gas is not circulated.

Therefore, the present embodiment is characterized in that the flash gas generated through the gas-liquid separator 40 is supplied to the upstream side of the evaporation gas heat exchanger 20 so that the evaporation gas supplied from the liquefied gas storage tank 10 to the evaporation gas heat exchanger 20 So that the liquefaction efficiency of the evaporated gas compressed by the first to fourth evaporative gas compressors 51 to 54 and returned to the evaporative gas heat exchanger 20 can be increased to 60% or more .

In the gas-liquid separator 40, the evaporated gas is separated into a liquid and a gas so that the liquid is supplied to the liquefied gas storage tank 10, and the gas is supplied as flash gas to the upstream side of the first to fourth evaporative gas compressors 51 to 54 Can be recovered.

That is, when the evaporated gas is separated into the liquid and the gas in the gas-liquid separator 40, the liquefied evaporated gas (liquid) and the flash gas (gas) are respectively supplied to the liquefied gas storage tank 10 ), Or may be recovered upstream of the evaporative gas heat exchanger 20 through the flash gas feed line L6.

As described above, the gas-liquid separator 40 in this embodiment recovers the liquefied evaporated gas to the liquefied gas storage tank 10 and supplies the flash gas generated in the gas-liquid separator 40 to the upstream side of the evaporative gas heat exchanger 20 The excess evaporation gas can be re-liquefied and restored in the liquefied gas storage tank 10, and the flash gas can be re-pressurized through the first to fourth evaporative gas compressors 51 to 54 without discarding the flash gas, 2 Demand (71,72) can be reused.

The first to fourth evaporative gas compressors 51 to 54 pressurize the evaporative gas generated in the liquefied gas storage tank 10 and supply the pressurized gas to the first and second consumers 71 and 72, L1, respectively.

The first to fourth evaporative gas compressors 51 to 54 can be connected in series by a plurality of stages (pistons) to pressurize the evaporation gas at multiple stages. For example, the first to fourth evaporative gas compressors 51 to 54 have a structure in which four or five pistons are connected in series, that is, connected in series at four or five stages. In the final stage, To about 350 bar (preferably about 306 bar), and can be discharged and supplied to the first customer 71.

The first return line L2 of the evaporation gas is branched between the first to fourth evaporative gas compressors 51 to 54 and the first demander 72 on the evaporation gas supply line L1 and is supplied to the evaporation gas heat exchanger 20). At this time, a valve (not shown) may be provided at the branching point on the evaporation gas supply line L1, and the valve may be connected to the evaporation gas heat exchanger 20 The flow rate of the supplied evaporating gas can be controlled, and it can be a three-way valve.

The first to fourth evaporative gas compressors 51 to 54 may be equipped with evaporative gas coolers (not shown) between their respective stages. When the evaporation gas is pressurized by the first to fourth evaporative gas compressors 51 to 54, the temperature may also rise in accordance with the pressure increase. Therefore, in this embodiment, the evaporation gas cooler is used to lower the temperature of the evaporation gas again You can give. The evaporation gas cooler may be installed in the same number as each stage of the first to fourth evaporative gas compressors 51 to 54. Each evaporative gas cooler is connected to each of the first to fourth evaporative gas compressors 51 to 54, As shown in FIG.

Also, the first to fourth evaporative gas compressors 51 to 54 may be a room-temperature evaporative gas compressor in which the temperature of the evaporative gas sucked in the first stage is minus 40 degrees to minus 20 degrees. To this end, a separate heating device (not shown) is required at the front end of the first to fourth evaporative gas compressors 51 to 54.

The heating apparatus may raise the temperature of the substantially-110 ° C. evaporation gas generated in the liquefied gas storage tank 10 from -40 ° C. to -20 ° C. to the first to fourth evaporative gas compressors 51 to 54 .

The evaporation gas branch line L3 is branched from the first stage to the second stage of the first to fourth evaporative gas compressors 51 to 54 on the evaporation gas supply line L1 so as to be connected to the second demander 72 Can be connected.

Here, the evaporated gas discharged from the first end of the first to fourth evaporative gas compressors 51 to 54 can be compressed at a low pressure of 4 bar to 6 bar and can be supplied to the second customer.

The first to fourth evaporative gas compressors 51 to 54 may be standard high pressure compressors (SHP compressors), for example. Here, the standard high-pressure compressor (SHP compressor) can be formed such that the cylinder is formed in a V-shape and the size of the compressor itself is considerably reduced, thereby drastically reducing the space occupied by the compressor.

The first customer 71 uses evaporative gas or liquefied gas from the liquefied gas storage tank 10 as fuel. At this time, the first customer 71 may be a high-pressure gas injection engine (for example, MEGI), and in the case of the MEGI engine, a pressurized gas at a high pressure of about 150 to 350 bar may be used as fuel.

As the piston (not shown) inside the cylinder (not shown) reciprocates by the combustion of the liquefied gas or the evaporative gas, the first customer 71 rotates the crankshaft (not shown) connected to the piston , The propeller shaft S connected to the crankshaft can be rotated. Therefore, as the propeller P connected to the propeller shaft S rotates when the first customer 71 is driven, the hull H can move forward or backward.

The first customer 71 is a two-stroke DF engine driven by a diesel cycle and may be a low-speed engine. In this diesel cycle, air is compressed by the piston, the compressed high-temperature air is ignited by a pilot fuel, and the remaining high-pressure gas is injected and exploded.

In this case, the ignition fuel uses HFO (Heavy Fuel Oil) or MDO (Marine Diesel Oil), the ratio of the ignition fuel to the high-pressure gas is about 5:95, and the injection amount of the ignition fuel is adjusted to 5 to 100% It is possible. Therefore, the ignition fuel is also usable as the driving fuel for the engine.

That is, when the injection amount of the ignition fuel is about 5%, evaporative gas (or heated liquefied gas; about 95%) is mainly used as the engine driving fuel, and when the injection amount of the ignition fuel is 100% Fuel (oil) is all used.

At this time, when the injection amount of the ignition fuel is about 50% (and about 50% of the evaporation gas), the ignition fuel and the evaporation gas are mixed and not ignited into the engine, but the ignition fuel is ignited first to generate a calorific value, Gas is generated and exploded to produce a calorific value to produce a calorific value necessary for driving the first customer 71. [

The second consumer site 72 uses the evaporative gas supplied from the liquefied gas storage tank 10 as fuel. That is, the second demanding customer 72 needs the evaporation gas and can be driven using it as a raw material. The second customer 72 may be, but is not limited to, a generator (e.g., DFDG), a gas-fired unit (GCU), a boiler (e.g.

Specifically, the second customer site 72 can be connected to the first to fourth evaporative gas compressors 51 to 54 through the evaporative gas branch line L3, and the first to fourth evaporative gas compressors 51 to 54 (2 to 8 bar; preferably 4 to 6 bar) at the first stage of the first stage of the reaction.

In addition, the second customer site 72 may be a heterogeneous fuel engine in which a heterogeneous fuel can be used, so that not only evaporation gas but also oil can be used as fuel. However, since the evaporation gas and oil are not mixed and supplied, As shown in FIG. This is to prevent the mixture of two materials having different combustion temperatures from being mixed, thereby preventing the efficiency of the second customer 72 from deteriorating.

In addition, the second customer 72 can generate steam by heating fresh water as a boiler, and store the generated steam in a separate steam storage medium.

The boiler 72 can supply the generated steam to a heater (shown in Figs. 2 and 3) 61 or a forced vaporizer (shown in Fig. 3) 62 through which the heater 61 or the forced vaporizer 62 to heat the evaporation gas.

The evaporation gas generation amount measuring sensor 85, the evaporation gas bypass first to fourth lines BL1 to BL4, the pressure sensor 831 and the flow rate sensor 832 in the embodiment of the present invention.

The evaporation gas generation amount sensor 85 can measure the amount of evaporation gas generated in the liquefied gas storage tank 10 and can measure the amount of the evaporation gas generated in the liquefied gas storage tank 10 according to the internal pressure of the liquefied gas storage tank 10 The amount of evaporation gas generated in the liquefied gas storage tank 10 can be calculated through the property value of the remaining evaporation gas.

In addition, the evaporation gas generation amount sensor 85 may be connected to the first control unit 90 in a wired or wireless manner to transmit the measured evaporation gas generation amount information to the first control unit 90.

The first to fourth lines BL1 to BL4 of the evaporation gas bypass are connected to the first to fourth evaporative gas compressors 51 to 54 on the evaporation gas supply line L1 having the first to fourth evaporative gas compressors 51 to 54, The first to fourth evaporative gas compressors 51 to 54 may be branched at the downstream ends of the first to fourth evaporative gas compressors 51 to 54, respectively.

The first to fourth lines BL1 to BL4 of the evaporation gas bypasses the first to fourth evaporative gas compressors 51 to 54 under the control of the first and second controllers 90 and 91 It is possible to bypass (return) at least a part of the evaporated gas to be discharged to the front ends of the first to fourth evaporative gas compressors 51 to 54.

Accordingly, the first to fourth lines (BL1 to BL4) of the evaporation gas bypasses the first to fourth evaporation gas compressors (51 to 54) when the predetermined time is exceeded in the standby state of the first to fourth evaporative gas compressors The first to fourth evaporative gas compressors 51 to 54 are enabled to operate (controlled by the first control unit 90), and in addition, (Control by the second control unit 91)

At this time, the first line BL1 of the evaporation gas bypass includes a pressure regulating valve 841 for regulating the pressure of the evaporation gas discharged from the first evaporation gas compressor 51, and the evaporation gas bypass second through fourth The lines BL2 to BL4 may further include first to third flow rate regulating valves 842 to 844 for regulating the flow rate of the evaporated gas discharged from the second to fourth evaporative gas compressors 52 to 54.

The opening control of each pressure regulating valve 841 and the first to third flow regulating valves 842 to 844 can be controlled by the second control unit 91.

The pressure sensor 831 and the flow rate sensor 832 are provided on the downstream side of the first to fourth evaporative gas compressors 51 to 54 on the evaporative gas supply line L1 and are connected to the first to fourth evaporative gas compressors 51 The pressure or the flow rate of the evaporated gas discharged from the evaporator can be measured.

Here, the pressure sensor 831 and the flow rate sensor 832 are connected to the second control unit 91 in a wired or wireless manner, so that information on the pressure or flow rate discharged from the first to fourth evaporative gas compressors 51 to 54 To the second control unit (91).

The first control unit 90 controls the first to fourth evaporative gas compressors 51 to 54 according to the amount of evaporative gas generated in the liquefied gas storage tank 10 and more specifically, At least one of the first to fourth evaporative gas compressors 51 to 54 is controlled to be in the standby state. Here, the standby state refers to a state including both an operation standby state or an operation stop state of the evaporative gas compressor in a state in which the compression of the evaporative gas is not realized.

Specifically, the first control unit 90 receives the evaporation gas generation amount measured from the evaporation gas generation amount measurement sensor 85 by wire or wireless, and controls the first to fourth evaporative gas compressors 51 to 54 have.

More specifically, when the evaporation gas generation amount received from the evaporation gas generation amount measurement sensor 85 is equal to or smaller than the predetermined generation amount, the first control unit 90 operates any one of the first to fourth evaporative gas compressors 51 to 54 And control to increase the remaining three loads of the first to fourth evaporative gas compressors 51 to 54 connected in parallel. For example, the first control unit 90 controls the first evaporative gas compressor 51 to stand by when the evaporative gas generation amount transmitted from the evaporative gas generation amount measurement sensor 85 is equal to or less than the predetermined generation amount, It is possible to control the load of the fourth evaporative gas compressor 52 to 54 to be increased.

Of course, when the evaporation gas generation amount received from the evaporation gas generation amount measurement sensor 85 exceeds the preset generation amount, the first control unit 90 may be configured to activate all of the first to fourth evaporative gas compressors 51 to 54 Can be controlled.

The first control unit 90 closes the evaporation gas first flow rate valve 81a and opens the evaporation gas second flow rate valve 81b to open the evaporation gas second flow rate valve 81b to the liquefied gas storage tank 10 to be supplied to the first to fourth evaporative gas compressors 51 to 54 by bypassing the evaporative gas heat exchanger 20 through the evaporative gas bypass line L7, The evaporated gas first flow valve 81a is opened and the evaporated gas second flow valve 81b is closed so that the evaporated gas supplied from the liquefied gas storage tank 10 is supplied to the evaporation gas heat exchange It is possible to control the partial re-liquefaction of the evaporated gas compressed in the first to fourth evaporative gas compressors 51 to 54 through the unit 20.

Here, the predetermined generation amount is the amount of evaporative gas flowing into the first to fourth evaporative gas compressors 51 to 54 at the ineffective point A of the first to fourth evaporative gas compressors 51 to 54.

The inefficiency point A is set such that even if the flow rate supplied to the first to fourth evaporative gas compressors 51 to 54 is reduced in proportion to the flow rate of the flow rate of the first to fourth evaporative gas compressors 51 to 54 And the flow rates of the first to fourth evaporative gas compressors 51 to 54 at the points where the power is not reduced. The flow rate of the inefficient point A of the first to fourth evaporative gas compressors 51 to 54 can be a flow rate of 20 to 40% of the flow rate at which the first to fourth evaporative gas compressors 51 to 54 have the maximum load have.

The details of this will be described in detail with reference to FIG.

4 is a graph illustrating power consumption versus flow rate of an evaporative gas compressor according to an embodiment of the present invention.

As shown in the graph of FIG. 4, in the first to fourth evaporative gas compressors 51 to 54, when the flow rate is the ineffective point (A) or more, power consumption increases proportionally as the flow rate increases. This means that a large amount of power is required to compress the evaporated gas at a large flow rate. At this time, the inefficiency point A is a flow rate value determined according to the specifications of the first to fourth evaporative gas compressors 51 to 54, the driving conditions, etc., and the first to fourth evaporative gas compressors 51 to 54 are the maximum load The flow rate is 20 to 40% of the flow rate.

On the other hand, in the section where the flow rate of the evaporative gas flowing into the first to fourth evaporative gas compressors 51 to 54 is less than the ineffective point A, the power consumption is not reduced even if the flow rate is reduced. This is due to the power consumption consumed to prevent surging which would occur if a certain volume of evaporative gas was not introduced into the first to fourth evaporative gas compressors 51 to 54.

That is, a part of the evaporation gas flowing into the first to fourth evaporation gas compressors 51 to 54 is recycled to increase the evaporation gas flow volume to the first to fourth evaporation gas compressors 51 to 54 by a predetermined value or more It is possible to prevent the first to fourth evaporative gas compressors 51 to 54 from surging. At this time, in order to perform recycling, separate power consumption is generated in the first to fourth evaporative gas compressors 51 to 54. Because of this power consumption, they are introduced into the first to fourth evaporative gas compressors 51 to 54 Even if the evaporation gas amount is reduced, the power consumption is not reduced.

 Therefore, in the embodiment of the present invention, when the first to fourth evaporative gas compressors 51 to 54 are driven in parallel, the characteristics of the first to fourth evaporative gas compressors 51 to 54 The power consumed by the first to fourth evaporative gas compressors 51 to 54 can be minimized.

That is, in the embodiment of the present invention, at least one of the first to fourth evaporative gas compressors 51 to 54 is operated when the evaporation gas generation amount is equal to or less than a predetermined value (this time is shorter than the point A shown in FIG. 4) It is possible to prevent the waste of power consumption by increasing the load of the remaining evaporative gas compressor.

For example, if the flow rate of the inefficient point (A) is 50 and the power consumption at that time is 50, and the ratio of the flow rate to the power consumption (slope) is 1 (based on one evaporative gas compressor) (When the amount of evaporated gas generated in the liquefied gas storage tank 10 is equal to or smaller than the preset amount of generation), the flow rate of the evaporation gas flowing into the first to fourth evaporative gas compressors 51 to 54 is 30, The case where both of the first to fourth evaporative gas compressors 51 to 54 are driven and the case where the power consumption when the first evaporative gas compressor 51 of the first to fourth evaporative gas compressors 51 to 54 Let's compare them.

1), the first to fourth evaporative gas compressors 51 to 54 are all driven, so that the power consumption is 50 * 4 = 200. However, in case 2), the driving of the first evaporative gas compressor 51 is stopped and the evaporative gas is further supplied to the remaining second to fourth evaporative gas compressors 52 to 54 at a flow rate of 10, resulting in 60 * 3 = 180.

That is, the driving of 2) compared to 1) becomes very efficient in terms of power consumption of the evaporative gas compressor.

As described above, in the embodiment of the present invention, when the first to fourth evaporative gas compressors 51 to 54 are driven in parallel, when the evaporative gas generation amount is equal to or less than the predetermined generation amount, the first to fourth evaporative gas compressors 51 To 54), it is possible to minimize the power consumed by the first to fourth evaporative gas compressors 51 to 54.

The first control unit 90 may control at least one of the plurality of evaporative gas compressors 51 to 54 to be in the standby state alternately when the evaporative gas generation amount is repeatedly generated below the predetermined generation amount.

Specifically, the first control unit 90 controls at least one of the first to fourth evaporative gas compressors 51 to 54 to be in a standby state when the evaporation gas generation amount is equal to or less than the preset generation amount, The remaining one of the first to fourth evaporative gas compressors 51 to 54 can be controlled to be in the standby state.

For example, the first control unit 90 controls the first evaporative gas compressor 51 to be in the standby state and the second to fourth evaporative gas compressors 52 to 54 to the standby state when the evaporative gas generation amount is equal to or smaller than the pre- .

The first control unit 90 releases the standby state of the first evaporative gas compressor 51 and restarts the first evaporative gas compressor 51 so that the first to fourth evaporative gas compressors 51 - 54 are all activated.

Next, when the evaporation gas generation amount changes again to a predetermined amount or less, the second evaporative gas compressor (52) other than the first evaporative gas compressor (51) is controlled to be in an operation stop state and the first, third and fourth The evaporative gas compressors (51, 53, 54) are controlled so as to remain in the operating state.

Therefore, in the embodiment of the present invention, the durability of the first to fourth evaporative gas compressors 51 to 54 can be improved by performing the above-described alternate control through the first controller 90.

Further, the first control unit 90 controls at least one of the first to fourth evaporative gas compressors 51 to 54 to be in an operation stop state, and controls the evaporated gas compressor, which has stopped operating, do.

Here, the first control unit 90 controls the evaporative gas compressor 51, which is waiting for operation, to operate when the standby state of the evaporative gas compressor (for example, the first evaporative gas compressor 51) Or to restart the evaporated gas compressor 51 which is in the standby state for operation and to start the operation of the evaporative gas compressor 51 which has started to operate through the evaporative gas compressor bypass line (for example, the evaporative gas compressor bypass first line BL1) The evaporation gas compressor bypass lines BL1 to BL4 are each provided with a control valve (not shown), and each of the evaporation gas compressor bypass lines BL1 to BL4 is provided with a control valve The first control unit 90 may perform the bypass control through the control valve.

Here, the preset condition may be a condition that reaches the time before the operation of the evaporated gas compressor 51 is restarted at the time for restarting the operation of the evaporated gas compressor 51, The time point at which the evaporative gas compressor 51 restarts is a time point when the internal pressure of the liquefied gas storage tank 10 exceeds the preset pressure or when the evaporated gas generation amount generated in the liquefied gas storage tank 10 exceeds the predetermined amount Lt; / RTI >

As described above, in the embodiment of the present invention, the first to fourth evaporative gas compressors 51 to 54 can be quickly returned from the standby state to the operating state through the first control unit 90, thereby improving reliability of the evaporative gas supply The stability is maximized.

The second control unit 91 controls the pressure of the evaporation gas discharged from the first to fourth evaporative gas compressors 51 to 54 in accordance with the pressure or flow rate of the evaporation gas required by the first and second consumers 71 and 72 Or the flow rate.

Specifically, the second control unit 91 compares the pressure or flow rate of the evaporation gas requested by the first customer 71 with the pressure or flow rate measured by the pressure sensor 831 and the flow rate sensor 832, Controls only the pressure of the evaporated gas discharged to only one evaporative gas compressor of the first to fourth evaporative gas compressors 51 to 54, and the flow rate is controlled by the first to fourth evaporative gas compressors 51 Only the flow rate of the evaporated gas discharged to the evaporative gas compressor other than the evaporative gas compressor of one of the evaporative gas compressors is controlled.

For example, when the pressure of the evaporation gas requested by the first customer 71 is lower than the pressure measured by the pressure sensor 831, the second control unit 91 closes the pressure regulating valve 841, When the pressure of the evaporation gas required by the first customer 71 is higher than the pressure measured by the pressure sensor 831, the pressure regulating valve 842 is opened So that at least a part of the evaporative gas discharged from the first evaporative gas compressor 51 through the first line BL1 of the evaporative gas compressor bypass can be controlled to be supplied to the upstream side of the first evaporative gas compressor 51. (Pressure control)

When the flow rate of the evaporation gas requested by the first customer 71 is larger than the flow rate measured by the flow rate sensor 832, the second control unit 91 controls the first to third flow rate control valves 842 to 844 And controls the load of the second to fourth evaporative gas compressors 52 to 54 to be increased. When the flow rate of the evaporative gas required by the first customer 71 is less than the flow rate measured by the flow rate sensor 832 The first to third flow rate regulating valves 842 to 844 are opened and the second to fourth evaporative gas compressors 52 to 54 are connected to the second to fourth lines BL2 to BL4 through the evaporative gas compressor bypasses It is possible to control to supply at least a part of the evaporated gas to be discharged to the front ends of the second to fourth evaporative gas compressors 52 to 54.

As described above, in the embodiment of the present invention, even when the first to fourth evaporative gas compressors 51 to 54 are driven in parallel through the second control unit 91, the pressure or the flow rate required by the first customer 71 So that the reliability of the supply of the evaporation gas is improved and the stability is maximized.

2 is a conceptual diagram of a gas processing system according to another embodiment of the present invention.

2, the gas processing system 2 according to another embodiment of the present invention includes a liquefied gas storage tank 10, an evaporation gas heat exchanger 20, an evaporation gas decompressor 30, a gas- A first customer 41, a second customer 34, and a third control unit 40. The first to fourth evaporative gas compressors 51 to 54, the heater 61, the first customer 71, the second customer 72,

The configurations except for the heater 61 and the third control unit 92 in the embodiment of the present invention are the same as those in the gas processing system 2 according to the embodiment of the present invention described with reference to FIG. Reference numerals are used to designate the same or similar components.

Hereinafter, a gas processing system 2 according to another embodiment of the present invention will be described with reference to FIG. 2, and the heater 61 and the third control unit 92 will be mainly described.

The heater 61 is provided on the evaporation gas bypass line L7 and bypasses the evaporation gas heat exchanger 20 to heat the evaporation gas supplied to the first to fourth evaporation gas compressors 51 to 54 do.

The heater 61 can receive steam supplied from the boiler 72 as a heat source and heat exchange between the steam and the evaporation gas generated in the liquefied gas storage tank 10, The temperature can be raised from 40 degrees to -20 degrees.

In the embodiment of the present invention, the evaporation gas temperature measurement sensor 86 may be further included.

The evaporation gas temperature sensor 86 may be provided downstream of the evaporation gas heat exchanger 20 on the evaporation gas supply line L1 and upstream of the first to fourth evaporation gas compressors 51 to 54, 1 to the fourth evaporative gas compressors 51 to 54, and transmit the measured temperature of the evaporated gas to the third control unit 92.

Here, the evaporation gas temperature sensor 86 may be connected to the third control unit 92 in a wired or wireless manner.

The third control unit 92 controls the flow rate of the evaporation gas supplied to the evaporation gas heat exchanger 20 and the heater 61 according to the amount of evaporation gas generated in the liquefied gas storage tank 10.

Specifically, the third control unit 92 controls the evaporation gas supplied from the liquefied gas storage tank 10 to be supplied only to the heater 61 when the evaporation gas generation amount is equal to or less than the first predetermined amount, The evaporation gas supplied from the liquefied gas storage tank 10 is controlled to be supplied to both the evaporation gas heat exchanger 20 and the heater 61 when the amount of evaporation gas generated is less than the first set generation amount, It is possible to control the evaporation gas supplied from the liquefied gas storage tank 10 to be supplied only to the evaporation gas heat exchanger 20 in the case where the amount is the second predetermined amount. Here, the first predetermined amount is less than the second predetermined amount.

The details of this will be described in detail with reference to FIG.

5 is a graph showing the amount of evaporative gas generated in the liquefied gas storage tank versus the operating time of the ship according to the embodiment of the present invention.

As shown in the graph of Fig. 5, the amount of evaporation gas generated in the liquefied gas storage tank 10 changes according to the operating time of the ship 1.

Specifically, the amount of the evaporation gas generated in the liquefied gas storage tank 10 increases continuously at a constant rate in the initial period B1 of the operation and the middle period B2 of the operation. In the mid-flight section (B3), the amount of evaporative gas generation increases at a certain rate in the early stage, and the amount of evaporation gas decreases at a certain rate in the latter half of the period. Finally, in the last period (B2) and the last period (B1), the amount of evaporative gas generation is continuously reduced at a constant rate.

Here, the initial cruising period B1 and the cruising period B1 are equal to or less than the first predetermined amount X, and the initial cruising period B2 and the cruising period B2 are the first predetermined amount X ), And the mid-flight section B3 is a section that is equal to or larger than the second predetermined amount Y of generation.

As described above, in the embodiment of the present invention, considering the change in the amount of evaporation gas generated in the liquefied gas storage tank 10 according to the operating time of the ship 1, the first to fourth The preheating drive control of the evaporation gas flowing into the evaporation gas compressors 51 to 54 is optimized.

Specifically, the third control unit 92 determines whether the amount of evaporation gas generated in the liquefied gas storage tank 10 is equal to or less than the first preset amount X of generation The opening degree of the evaporation gas second flow rate valve 81b is opened and the evaporation gas supplied from the liquefied gas storage tank 10 is supplied only to the heater 61. [

When the evaporated gas generation amount generated in the liquefied gas storage tank 10 is less than the second predetermined set generation amount Y exceeding the first predetermined generation amount X (in the section B2), the third control unit 92 controls the evaporation gas The opening of both the first and second flow rate valves 81a and 81b is opened so that the evaporation gas supplied from the liquefied gas storage tank 10 is supplied to the evaporation gas heat exchanger 20 and the heater 61, The opening ratio between the first and second flow rate valves 81a and 81b can be controlled according to the temperature measured by the gas temperature measuring sensor 86. [

The third control unit 92 opens the opening of the evaporation gas first flow rate valve 81a when the evaporation gas generation amount generated in the liquefied gas storage tank 10 is equal to or larger than the second predetermined generation amount Y And the opening of the evaporation gas second flow rate valve 81b is closed so that the evaporation gas supplied from the liquefied gas storage tank 10 is supplied only to the evaporation gas heat exchanger 20. [

As described above, in the embodiment of the present invention, the evaporation gas heat exchanger 20 controls the preheating drive of the evaporation gas flowing into the first to fourth evaporative gas compressors 51 to 54 according to the operating time of the ship 1, It is possible to prevent malfunctions of the first to fourth evaporative gas compressors 51 to 54, which may occur when only the first to fourth evaporative gas compressors 51 to 54 are present, thereby improving the reliability of the system.

3 is a conceptual diagram of a gas processing system according to another embodiment of the present invention.

3, the gas processing system 2 according to another embodiment of the present invention includes a liquefied gas storage tank 10, an evaporation gas heat exchanger 20, an evaporation gas decompressor 30, The first vaporizer 61, the second vaporizer 62, the pump 63, the first customer 71, the second customer 72, and the second vaporizer 72. The separator 40, the first to fourth evaporative gas compressors 51 to 54, the heater 61, 4 control unit 93, as shown in FIG.

In the embodiment of the present invention, the configurations other than the forced vaporizer 62, the pump 63 and the fourth control unit 93 are the same as those of the gas processing system 2 according to the embodiment of the present invention ), The same reference numerals are used for convenience of description and the like, but they are not necessarily referred to by the same reference numerals.

The gas treatment system 2 according to another embodiment of the present invention will now be described with reference to FIG. 3 and the description of the forced vaporizer 62, the pump 63 and the fourth control unit 93 will be focused on do.

In the embodiment of the present invention, it is possible to further include a forced evaporation gas supply line L8.

The forced evaporation gas supply line L8 connects the liquefied gas storage tank 10 and the evaporation gas heat exchanger 20 downstream of the evaporation gas supply line L1 and may include a forced vaporizer 62.

The forced evaporation gas supply line L8 may be provided with an additional evaporation gas supply valve 82 and the supply amount of the liquefied gas supplied to the forced vaporizer 62 in accordance with the opening degree control of the additional evaporation gas supply valve 82 Lt; / RTI >

Here, the evaporation gas addition supply valve 82 may be connected to the fourth control unit 93 in a wired or wireless manner to receive the opening adjustment command of the fourth control unit 93.

The forced vaporizer 62 is provided on the forced evaporation gas supply line L8 and supplies the liquefied gas stored in the liquefied gas storage tank 10 from the pump 63 to the forced vaporization, (51-54).

The forced vaporizer 62 can receive the steam supplied from the boiler 72 as a heat source and heat exchange the steam and the evaporation gas generated in the liquefied gas storage tank 10 to supply the liquid liquefied gas to the vapor phase It can be phase-changed to a forced vaporization evaporation gas.

At this time, the liquefied gas in the liquid state can be raised to a forced vaporized gas having a temperature of about -163 degrees Celsius, and the liquefied gas has a temperature of from -40 degrees to -20 degrees. This is because the phase change from the liquid phase to the gas phase Accompanied.

The forced vaporizer 62 can share the steam with the heater 61. Specifically, the boiler 72 can supply steam to the forced vaporizer 62 as well as the heater 61.

Further, the forced vaporizer 62 can be driven together with the heater 61.

The reason why the heater 61 is driven in the embodiment of the present invention is that the preheating function of the evaporation gas heat exchanger 20 is weakened and must be supplemented. That is, in this case, the amount of evaporation gas generated in the liquefied gas storage tank 10 is reduced. As a result, the amount of the evaporation gas to be supplied to the first to fourth evaporative gas compressors 51 to 54 is small Loses.

Therefore, in the embodiment of the present invention, the forced vaporizer 62 and the heater 61 may be driven together to supplement the amount of the evaporative gas to be supplied to the first to fourth evaporative gas compressors 51 to 54. As a result, the driving reliability of the first to fourth evaporative gas compressors 51 to 54 can be improved.

That is, the forced vaporizer 62 and the heater 61 use steam as a heat exchange medium. By sharing the steam with each other, the position where the equipment is installed can be shared. Details thereof will be described later.

The pump 63 can supply the liquefied gas stored in the liquefied gas storage tank 10 to the forced vaporizer 62 provided on the forced evaporation gas supply line L8.

The pump 63 is connected to the fourth control unit 93 in a wired or wireless manner and can receive the pump operation signal or the pump shutdown signal. The pump 63 is operated by the pump operation signal of the fourth control unit 93, The supply of the liquefied gas stored in the storage tank 10 to the forced vaporizer 62 or the supply of the liquefied gas to the forced vaporizer 62 is stopped by the pump shutdown signal.

Here, the pump 63 may be provided inside or outside the liquefied gas storage tank 10, and may be a centrifugal pump, for example.

The fourth control unit 93 controls the flow rate of the evaporation gas supplied to the evaporation gas heat exchanger 20 and the heater 61 and the flow rate of the evaporation gas supplied to the forced vaporizer 62 according to the amount of evaporation gas generated in the liquefied gas storage tank 10 The flow rate of the liquefied gas can be controlled.

Specifically, the fourth control unit 93 drives the heater 61 and the forced vaporizer 62 together when the evaporation gas generation amount is equal to or less than the first predetermined amount, and controls the evaporation gas heat exchanger 20 not to operate And controls the heater 61 and the forced vaporizer 62 to operate together but also to operate the evaporation gas heat exchanger 20 when the evaporation gas generation amount is less than the first predetermined generation excess amount, When the amount of generation is equal to or more than the second predetermined amount of generation, only the evaporation gas heat exchanger 20 can be controlled to be operated.

The detailed control will be described with reference to FIG. 5, and the detailed description of FIG. 5 has been described above.

The fourth control section 93 closes the opening of the evaporation gas first flow rate valve 81a and opens the evaporation gas second flow rate valve 81b when the evaporation gas generation amount is equal to or less than the first predetermined generation amount X So that the evaporation gas supplied from the liquefied gas storage tank 10 is supplied only to the heater 61. The opening of the evaporation gas addition supply valve 82 is opened and the pump 63 is operated to supply the liquefied gas It is possible to control the liquefied gas stored in the storage tank 10 to be supplied to the forced vaporizer 62.

The fourth control section 93 determines whether or not the evaporated gas first flow rate valve 81a and the evaporated gas second evaporated gas second flow rate 81a are in a case where the evaporated gas generation amount is less than the first predetermined generation amount X and the second predetermined generation amount Y The opening of the flow rate valve 81b is all opened so that the evaporation gas supplied from the liquefied gas storage tank 10 is supplied to both the evaporation gas heat exchanger 20 and the heater 61. The evaporation gas addition supply valve 82 And the pump 63 is operated to control the liquefied gas stored in the liquefied gas storage tank 10 to be supplied also to the forced vaporizer 62. [ At this time, the fourth control section 93 opens the first and second evaporation gas flow rate valves 81a and 81b and the evaporation gas addition supply flow rate valve 82 according to the temperature measured by the evaporation gas temperature measurement sensor 86 The temperature of the evaporation gas supplied to the first to fourth evaporative gas compressors 51 to 54 can be controlled.

The fourth control section 93 opens the opening of the evaporation gas first flow rate valve 81a and opens the evaporation gas second flow rate valve 81b when the evaporation gas generation amount is equal to or larger than the second predetermined generation amount Y So that the evaporation gas supplied from the liquefied gas storage tank 10 is supplied only to the evaporation gas heat exchanger 20 while the opening of the evaporation gas addition supply valve 82 is closed and the pump 63 is operated So that the liquefied gas stored in the liquefied gas storage tank 10 can be prevented from being supplied to the forced vaporizer 62.

As described above, in the embodiment of the present invention, the preheating drive of the evaporation gas flowing into the first to fourth evaporative gas compressors 51 to 54 is controlled in accordance with the operating time of the ship 1, and the forced vaporizer 62 The flow rate of the evaporation gas flowing into the first to fourth evaporation gas compressors 51 to 54 can be always adequately satisfied and the efficiency of driving the first to fourth evaporation gas compressors 51 to 54 can be maximized And the reliability of the system is improved.

Fig. 6 is a side view of a ship having a gas treatment system according to an embodiment of the present invention, Fig. 7 is an internal plan view of a cargo compressor room of a ship according to an embodiment of the present invention, Fig. FIG. 9 is an internal cross-sectional view of a cargo compressor room of a ship according to another embodiment of the present invention, and FIG. 10 is a sectional view of a cargo compressor room of a ship according to another embodiment of the present invention. Fig.

6 to 10, a ship 1 equipped with a gas processing system 2 according to an embodiment of the present invention includes a cargo compressor room 100, a skid 101, a motor room 200, An engine casing 300, a liquefied gas storage tank 10, first to fourth evaporative gas compressors 51 to 54, a first customer 71, and a second customer 72.

In the embodiment of the present invention, configurations other than the cargo compressor room 100, the skid 101, the motor room 200 and the engine casing 300 are the same as those of the embodiment of the present invention described with reference to FIGS. The same reference numerals are used for the respective constructions in the gas processing system 2 according to the first embodiment, but they are not necessarily referred to the same constructions.

Here, the first to fourth evaporative gas compressors 51 to 54 may be divided into a driving evaporative gas compressor and a blow-by gas evaporative gas compressor, which are the same as the first embodiment of the present invention described with reference to FIGS. 1 to 3 As described in the example of the gas treatment system 2, the evaporative gas compressor to be in operation standby is a heat-exclusive evaporative gas compressor, and the evaporative gas compressor that is always in operation standby mode and can be operated is a evaporative gas compressor for driving. For example, the driving evaporative gas compressor may be the first to third evaporative gas compressors 51 to 53, and the blowdown evaporative gas compressor may be the fourth evaporative gas compressor 54.

In the embodiment of the present invention described below, the first to fourth evaporative gas compressors 51 to 54 are provided in the gas processing system 2 according to the embodiment of the present invention described with reference to FIGS. 1 to 3 The described alternation control is not performed.

Hereinafter, with reference to FIG. 6, a description will be given of a ship 1 having a gas processing system 2 according to an embodiment of the present invention.

The vessel 1 can accommodate the liquefied gas storage tank 10 and the first and second consumers 71 and 72 in the hull H below the upper deck (not shown) A compressor room 100, a motor room 200, and an engine casing 300.

The ship 1 can be provided with a plurality of liquefied gas storage tanks 10 only in the inside of the hull H in the case of an LNG carrier depending on the transportation purpose and the cargo compartment 100, The liquefied gas storage tank 10, the cargo compresor room 100, the motor room 200, and the container accommodating holders 200, 200, and the engine casing 300 may be provided in the case of a container carrier, And an engine casing 300 and containers may be provided on the upper deck.

The embodiment of the present invention is not limited to the case of an LNG carrier, but for convenience of description, the case where the ship 1 is an LNG carrier will be described as an example.

The cargo compressor room 100 is a separate space provided on the upper deck of the hull H and may be provided in front of the motor room 200 as an example.

In addition, the cargo compressor room 100 is arranged long in a row only in the width direction of the ship H, and accommodates the first to fourth evaporative gas compressors 51 to 54 therein.

That is, the interior space of the cargo compressor room 100 is limited. On the other hand, as the throughput of the evaporative gas gradually increases, the first to fourth evaporative gas compressors 51 to 54 gradually use the space inside the cargo compressor room 100 as the compression capacity and the size gradually increase.

Therefore, in the embodiment of the present invention, the first to fourth evaporative gas compressors 51 to 54 have a height of one half of the height of the cargo compressor room 100, preferably within a range of 2 to 4 m, And an evaporative gas compressor having the same performance as the compressors. That is, the first to fourth evaporative gas compressors 51 to 54 may be standard high pressure compressors. At this time, the pistons of the first to fourth evaporative gas compressors 51 to 54, And a plurality of V-shaped crossing portions may be connected in series.

The first to fourth evaporative gas compressors 51 to 54 are formed by connecting a plurality of pistons in a V-shape so as to be connected in series to each other and have a height of 2 to 4 m or less. As a result, the cargo- ) To achieve optimal placement.

Specifically, in the first to fourth evaporative gas compressors 51 to 54, the first and second evaporative gas compressors 51 and 52 are disposed on the upper side and the third and fourth evaporative gas compressors 53 and 54 are disposed on the lower side The first and second evaporative gas compressors 51 and 52 can be arranged in the cargo compressor room 100 in a two-layered structure in which the space inside the cargo compressor room 100 occupied by the existing first and second evaporative gas compressors 51, Can be secured.

The cargo compressor room 100 is provided with the evaporation gas heat exchanger 20, the evaporation gas decompressor 30, the gas-liquid separator 40, the first to fourth evaporative gas compressors 51 to 54, A heater 61, a forced vaporizer 62, and the like, as well as a skid 101 to be described later.

Therefore, in the embodiment of the present invention, the inner space of the ship 1 can be optimized and used, and an extra space is generated, thereby improving the transportation ability.

Here, the heater 61 is disposed above the first to fourth evaporative gas compressors 51 to 54 when the first to fourth evaporative gas compressors 51 to 54 are disposed in the same layer other than the laminated structure .

The skid 101 is a flat support plate provided to support the first to fourth evaporative gas compressors 51 to 54 from the upper deck, and is provided in the cargo compressor room 100. Here, the skid can be mixed with the support plate and has the same meaning.

The skid 101 is a device for supporting the unstable evaporative gas compressors (for example, the first to third evaporative gas compressors 51 to 53) of the first to fourth evaporative gas compressors 51 to 54 from the upper deck A second support plate 101b for supporting a stand-by evaporation gas compressor (for example, a fourth evaporative gas compressor) 54 among the first support plate 101a and the first to fourth evaporative gas compressors 51 to 54 from the upper deck .

At this time, the first support plate 101a and the second support plate 101b may be separated from each other to the left and the right as shown in FIGS. 7 and 8 to form the vibration isolating gap 102.

7, when the first to fourth evaporative gas compressors 51 to 54 are arranged in a 4 * 1 matrix, the first to third evaporative gas compressors 51 to 53 And the second support plate 101b that supports the fourth evaporative gas compressor 54. The amount of evaporative gas generated in the liquefied gas storage tank 10 is set to be greater than the amount of evaporated gas generated in the liquefied gas storage tank 10, It is possible to shut off the vibrations generated by the operation of the first to third evaporative gas compressors 51 to 53 when the fourth evaporative gas compressor 54 is put on standby.

As a result, in the embodiment of the present invention, the stand-by evaporative gas compressor 54 can be protected from vibration, and durability is improved.

8, when the first to fourth evaporative gas compressors 51 to 54 are arranged in a 2 * 2 matrix, the first to third evaporative gas compressors 51 Between the first support plate 101a supporting the first evaporation gas compressor 54 and the second support plate 101b supporting the fourth evaporation gas compressor 54, The vibration generated by the first to third evaporative gas compressors 51 to 53 can be cut off when the evaporative gas generation amount falls below the preset amount and the fourth evaporative gas compressor 54 is in standby mode.

At this time, the vibration isolating gap 102 may include a member for attenuating vibration, for example, air or a separate damper.

The skid 101 also includes an upper skid 101u and a third and fourth evaporative gas compressors 53 and 54 that support the first and second evaporative gas compressors 51 and 52 spaced upward from the upper deck, ) From the upper deck.

9 and 10, the upper skid 101u and the lower skid 101l may be spaced apart from each other as shown in FIGS. 9 and 10, and the upper skid 101u is spaced upward from the upper deck 101a by the spacing member 103, As shown in FIG.

Here, the heater 61 may be provided on the upper skid 101u together with the first evaporative gas compressor 51, in which case the second evaporative gas compressor 52 is connected to the third and fourth evaporative gas compressors 53 And 54, respectively, in the lower skid 101l.

The spacing member 103 may connect the upper skid 101u with the upper skid 101u so that the upper skid 101u is spaced upward from the upper deck at a predetermined interval and connect the upper skid 101u with the upper deck.

In the case where the spacer member 103 connects the lower skid 101l and the upper skid 101u, the lower skid 101l corresponds to the upper deck portion corresponding vertically to the position of the spacing member 103 connected to the upper skid 101u. So that the spacer 103 can be vertically connected to the upper deck.

When the upper skid 101u and the lower skid 101l have the same area and shape when the spacer 103 connects the lower skid 101l and the upper skid 101u, It can be connected to the upper deck in the form of an oblique line.

Here, the spacing member 103 may include a vibration damping portion (not shown). The vibration damping portion may be a hydraulic damping device or an elastic body formed of an elastic material.

The motor room 200 can accommodate a motor (not shown) for driving the first to fourth evaporative gas compressors 51 to 54 and the like in a separately isolated space provided on the upper deck of the ship H And is provided adjacent to the cargo compressor room 100. For example, the motor room 200 may be disposed behind the cargo compartment 100.

The motor room 200 should be isolated from the cargo compartment 100, which is a hazard zone, as a safety zone. Therefore, in the embodiment of the present invention, an isolation wall (not shown) is provided between the cargo compartment 100 and the motor room 200 so that the spark due to the operation of the motor is not generated in the cargo compartment 100 So that the stability of the ship 1 is secured.

The engine casing 300 is provided on the upper deck of the hull H and is provided with at least a part of an engine room (not shown) provided with the first demanding place 71 and the second demanding place 72, (Not shown) and vent mast (not shown).

The engine casing 300 discharges the exhaust gas discharged from the first customer 71 and the second customer 72 through the stack and supplies the air discharged from the cabin H or a cabin To the outside.

As described above, in the embodiment of the present invention, the gas processing system 2 is arranged to optimize the inner space of the ship H, thereby improving the utilization efficiency of the inner space of the ship H.

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it is to be understood that the same is by way of illustration and example only and is not to be construed as limiting the present invention. It is obvious that the modification and the modification are possible.

It will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit and scope of the invention as defined by the appended claims.

1: Ship 2: Gas treatment system
10: Liquefied gas storage tank 20: Evaporative gas heat exchanger
30: evaporation gas decompressor 40: gas-liquid separator
51: first evaporative gas compressor 52: second evaporative gas compressor
53: third evaporative gas compressor 54: fourth evaporative gas compressor
61: heater 62: forced vaporizer
63: Pump 71: High pressure consumer
72: low pressure demand point 81a: evaporation gas first flow valve
81b: evaporation gas second flow valve 82: evaporation gas addition supply valve
831: Pressure sensor 832: Flow sensor
841: Pressure regulating valve 842,843,844: Flow regulating valve
85: Evaporation gas generation amount measuring sensor 86: Evaporating gas temperature measuring sensor
90: first control unit 91: second control unit
92: third control section 93: fourth control section
100, 100a, 100b, 100c: cargo compressor room 101: skid
101a: a first supporting plate 101b: a second supporting plate
101u: upper skid 101l: lower skid
102: Gap for blocking vibration 103: Skid supporting member
200: motor room 300: engine casing
L1: evaporation gas supply line L2: evaporation gas first return line
L3: Evaporative gas branch line L4: Evaporative gas second return line
L5: Re-liquefied gas return line L6: Flash gas supply line
L7: Evaporative gas bypass line L8: Forced evacuation gas supply line
BL1 to BL4: Evaporative gas compressor bypassing First to fourth lines
H: Hull S: Propeller shaft
P: Propeller

Claims (14)

An evaporative gas compressor provided with a plurality of evaporator gas compressors for supplying the evaporator gas generated from the liquefied gas storage tank to a customer and constructed in parallel with each other; And
And a controller for controlling the evaporative gas compressor according to an amount of evaporative gas generated in the liquefied gas storage tank,
Wherein,
A standby control for controlling at least one of the plurality of evaporative gas compressors to a standby state in which the evaporation gas is not compressed or a normal control for operating all of the plurality of evaporative gas compressors,
Wherein the evaporative gas compressor to be in the standby state in the standby control before and after the steady-
Wherein the gas processing system is different from the gas processing system. The apparatus of claim 1,
And controlling at least one of the plurality of evaporative gas compressors to be in the standby state when the evaporative gas generation amount is equal to or less than a predetermined generation amount,
And controls the remaining one of the plurality of evaporative gas compressors to be in the standby state when the evaporated gas generation amount becomes equal to or less than the preset generation amount. The compressor according to claim 1,
Characterized in that a four-stage or five-stage piston is connected in series with four constituent compressors, and the four constituent compressors are connected in parallel with each other. The method according to claim 1,
Further comprising an evaporation gas generation amount measuring sensor for measuring an evaporation gas generation amount generated in the liquefied gas storage tank,
Wherein,
And controls the driving of the evaporation gas compressor by receiving the evaporation gas generation amount measured by the evaporation gas generation amount measurement sensor. 5. The apparatus of claim 4,
Controls one of the evaporative gas compressors to be in the standby state when the evaporative gas generation amount received from the evaporative gas generation amount measurement sensor is equal to or less than a predetermined generation amount and controls the load of the remainder of the evaporative gas compressor connected in parallel to increase ,
And controls any one of the remainder of the evaporative gas compressor in which the load has been increased to be in the standby state when the evaporated gas generation amount again becomes equal to or less than the predetermined generation amount. The method according to claim 1,
An evaporation gas heat exchanger for exchanging heat between the evaporation gas supplied from the liquefied gas storage tank and the evaporation gas compressed by the evaporation gas compressor; And
Further comprising a bypass line for bypassing the evaporation gas heat exchanger,
Wherein,
Wherein the control unit controls the evaporation gas supplied from the liquefied gas storage tank to bypass the evaporation gas heat exchanger through the bypass line to be supplied to the evaporation gas compressor when the evaporation gas generation amount is equal to or less than a preset generation amount,
Wherein the evaporated gas supplied from the liquefied gas storage tank partially re-liquefies the evaporated gas compressed in the evaporated gas compressor through the evaporated gas heat exchanger when the evaporated gas generation amount exceeds the predetermined generation amount. 7. The method according to claim 6,
An evaporation gas amount flowing into the evaporation gas compressor at an inefficiency point of the evaporation gas compressor,
The inefficiency point of the evaporative gas compressor,
Wherein a ratio of a flow rate of power consumption of the evaporative gas compressor to a flow rate of power of the evaporative gas compressor is a point at which power consumption is not reduced even if the flow rate supplied to the evaporative gas compressor is reduced. 8. The method of claim 7, wherein the load at the inefficiency point of the evaporative gas compressor
Characterized in that the evaporative gas compressor is at a flow rate of 20 to 40% of the flow rate with a maximum load. The method according to claim 6,
An evaporative gas decompressor for decompressing the heat-exchanged evaporative gas supplied from the evaporative gas heat exchanger; And
Further comprising a gas-liquid separator for separating the reduced-pressure evaporated gas from the evaporated-gas decompressor into a liquid phase and a gaseous phase. 10. The system according to claim 9,
A high pressure consumer that consumes high pressure vapor of 150 to 350 bar; And
And a low pressure consumer consuming low pressure vapor of 4 to 8 bar. 11. The method of claim 10,
An evaporation gas supply line connecting the liquefied gas storage tank and the high-pressure consumer, and having the evaporative gas compressor;
An evaporation gas branch line branched at the intermediate stage of the evaporation gas compressor on the evaporation gas supply line and connecting the low-pressure consumer;
An evaporation gas first return line branched from the evaporation gas supply line downstream of the evaporation gas compressor and connecting the evaporation gas heat exchanger;
An evaporation gas second return line connecting the evaporation gas heat exchanger and the gas-liquid separator, the evaporation gas second return line including the evaporation gas decompressor;
A flash gas supply line connecting the gas-liquid separator and the evaporation gas heat exchanger upstream on the evaporation gas supply line; And
Further comprising a re-liquefied gas return line connecting said gas-liquid separator and said liquefied gas storage tank. The apparatus according to claim 4, wherein the evaporation gas generation amount measuring sensor comprises:
And the evaporation gas generation amount is calculated through the internal pressure of the liquefied gas storage tank. The compressor according to claim 1,
Characterized in that it is a Standard High Pressure Compressor. A vessel comprising the gas treatment system of any one of claims 1 to 6 and 8 to 13.

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