KR20190028097A - Gas Treatment System and Vessel having the same - Google Patents

Abstract

According to one embodiment of the present invention, a gas treatment system includes: a plurality of boil off gas compressors supplying a boil off gas generated from a liquefied gas storage tank to a demand source and provided in parallel with each other; and a buffer tank provided at the downstream of the boil off gas compressor. At least one of the boil off gas compressors is controlled in an operation halt state or a standby state which doesn′t implement compression of the boil off gas. The buffer tank temporarily stores the boil off gases discharged at different pressure in the plurality of boil off gas compressors so as to have predetermined pressure required by the demand source, and then supplies the boil off gases to the demand source.

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.

The present invention has been made to improve the prior art, and an object of the present invention is to provide a gas processing system and a ship including the same, which effectively supply liquefied gas and / or evaporated gas from a liquefied gas storage tank to a customer .

The gas processing system according to the present invention comprises: an evaporative gas compressor for supplying evaporated gas generated from a liquefied gas storage tank to a customer and provided in parallel to each other; And a buffer tank disposed downstream of the evaporative gas compressor, wherein the evaporative gas compressor is controlled to a standby state in which at least one of the evaporative gas compressors does not perform an operation stop or does not compress the evaporated gas, The evaporative gas compressor temporarily stores the evaporative gases discharged at different pressures to have the predetermined pressure required by the customer, and then supplies the evaporative gas to the customer.

Specifically, an evaporation gas supply line connecting the liquefied gas storage tank and the demander and having the evaporative gas compressor; A bypass line bypassing upstream from the buffer tank on the evaporation gas supply line; And at least one of the evaporative gas compressors is controlled to be in a standby state or in a standby state in which the compression of the evaporative gas is not implemented depending on the amount of evaporative gas generated in the liquefied gas storage tank, Wherein the control unit controls the evaporation gas flow downstream of the evaporation gas compressor according to the amount of the generated gas, and the control unit controls the flow rate of the evaporation gas discharged from the evaporation gas compressor when the evaporation gas generation amount generated in the liquefied gas storage tank is equal to or larger than the predetermined generation amount The control unit controls the evaporation gas to flow to the bypass line and controls the evaporation gas discharged from the evaporation gas compressor to flow to the buffer tank when the evaporation gas generation amount generated in the liquefied gas storage tank is less than a predetermined generation amount have.

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

Specifically, the apparatus further comprises evaporation gas first to fourth supply lines connecting the liquefied gas storage tank and the demander, and having the first to fourth evaporative gas compressors, wherein the first to fourth supply lines Upstream and downstream of the first to fourth evaporative gas compressors may be provided as an upstream common line and a downstream common line formed in common.

Specifically, the buffer tank may be provided on the downstream common line.

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 gas treatment system according to the present invention have an effect of effectively supplying liquefied gas and / or evaporated gas from a liquefied gas storage tank to a customer, thereby enhancing system stability and reliability.

1 is a conceptual view of a ship including a gas treatment system according to a first embodiment of the present invention.
2 is a conceptual view of a ship including a gas treatment system according to a second embodiment of the present invention.
3 is a conceptual view of a ship including a gas treatment system according to a third embodiment of the present invention.
4 is a conceptual view of a ship including a gas treatment system according to a fourth embodiment of the present invention.
5 is a conceptual view of a ship including a gas treatment system according to a fifth embodiment of the present invention.
6 is a conceptual view of a ship including a gas treatment system according to a sixth embodiment of the present invention.
7 is a conceptual view of a ship including a gas processing system according to a seventh embodiment of the present invention.
8 is a conceptual view of a ship including a gas treatment system according to an eighth embodiment of the present invention.
9 is a conceptual view of a ship including a gas processing system according to a ninth embodiment of the present invention.
10 is a conceptual view of a ship including a gas treatment system according to a tenth embodiment of the present invention.
11 is a conceptual view of a ship including a gas processing system according to an eleventh embodiment of the present invention.
12 is a graph of power consumption versus flow rate of an evaporative gas compressor according to an 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. It is also 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 respective drawings to be described below 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 1 of the present invention may be configured in combination with each other, and additions of the respective structures may be made to intersect each other. The gas processing system 1 according to an embodiment of the present invention may be mounted on a hull (not shown). In this case, the ship 100 may be a ship such as an LNG carrier, a container carrier, It does not.

The standby state described in the present specification refers to a state including both the standby state of operation of the evaporative gas compressor or the operation stop state in a state in which the compression of the evaporative gas is not implemented.

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

1 is a conceptual view of a ship including a gas treatment system according to a first embodiment of the present invention.

1, the gas processing system 1 according to the first embodiment of the present invention includes a liquefied gas storage tank 10, a boosting pump 20, a forced vaporizer 21, a preheater 30, A standard high-pressure evaporative gas compressor 40, a propulsion engine 50, and a control unit (not shown).

Hereinafter, a gas processing system 1 according to a first embodiment of the present invention will be described with reference to FIG.

Prior to describing the individual configurations of the gas processing system 1 according to the embodiment of the present invention, the basic flow paths for organically connecting the individual configurations 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.

The embodiment of the present invention may further include a forced gasification gas supply line L1, an evaporation gas supply line L2, and a first bypass line BL1. 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 forced gasification gas supply line L1 connects the liquefied gas storage tank 10 and the evaporation gas supply line L2 and includes a boosting pump 20 and a forced vaporizer 21 to supply the liquefied gas storage tank 10, Can be forcedly vaporized and supplied to the evaporation gas supply line (L2).

The evaporation gas supply line L2 is connected to the liquefied gas storage tank 10 and the propulsion engine 50 and includes a first pre-heater 30 and a standard high-pressure evaporative gas compressor 40, 10 may be supplied to the propulsion engine 50. At this time, the evaporation gas supply line L2 can connect the first to fifth evaporative gas compressors 41 to 45 in parallel, and the first to fifth evaporative gas compressors 41 to 45, May be referred to as first to fifth supply lines (not shown).

Since the evaporation gas supply lines L2 are formed in common upstream and downstream of the first to fifth supply lines, the upstream of the first to fifth supply lines can be referred to as the upstream common line, and the first to fifth The downstream of the feed line may be referred to as the downstream common line.

The first bypass line BL1 branches downstream of the standard high pressure evaporative gas compressor 40 on the evaporation gas supply line L2 and is connected upstream of the first preheater 30, So that the evaporated gas supplied from the liquefied gas storage tank 10 and compressed by the standard high-pressure evaporative gas compressor 40 can be supplied to the upstream of the first pre-heater 30 again. Here, the first control valve B1 may be connected to the control unit by wire or wirelessly, and receive the opening control command of the control unit.

Hereinafter, the individual components that are organically formed by the above-described respective lines (L1 to L3, BL1) to implement the gas processing system 1 will be described.

A liquefied gas storage tank (10) stores liquefied gas to be supplied to the propulsion engine (50). 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 a hull (not shown), and four liquefied gas storage tanks 10 may be formed in front of an 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 boosting pump 20 can supply the liquefied gas stored in the liquefied gas storage tank 10 to the forced vaporizer 21 provided on the forced vaporizing gas supply line L1.

The boosting pump 20 supplies the liquefied gas stored in the liquefied gas storage tank 10 to the forced vaporizer 21 or the liquefied gas supplied to the forced vaporizer 21 according to the required amount of fuel required by the propulsion engine 50 The supply of the gas can be stopped.

Here, the boosting pump 20 may be provided inside or outside the liquefied gas storage tank 10, and may be a centrifugal pump, for example.

The forced vaporizer 21 is provided on the forced vaporizing gas supply line L1 and supplies the liquefied gas stored in the liquefied gas storage tank 10 from the boosting pump 20 to the forced vaporizing gas supply line L1, ).

The forced vaporizer 21 can receive steam supplied from a boiler (not shown) as a heat source and heat-exchange the steam and the evaporated gas generated in the liquefied gas storage tank 10, It can be phase-changed into forced vaporization of vapor. Here, it goes without saying that various heat sources other than steam may be used as the heat source used in the forced vaporizer 21.

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 21 can share steam with the preheater 30. Specifically, the boiler can supply steam to the preheater 30 as well as to supply the steam to the forced vaporizer 21.

The preheater 30 is disposed upstream of the standard high-pressure evaporative gas compressor 40 on the evaporative gas supply line L2 and preheats the evaporative gas discharged from the liquefied gas storage tank 10 and supplies it to the standard high-pressure evaporative gas compressor 40 ).

The preheater 30 can receive the steam supplied from the boiler as a heat source and exchange heat between the steam and the evaporation gas generated in the liquefied gas storage tank 10 to reduce the evaporation gas at about minus 110 degrees to minus 40 degrees It is possible to raise the temperature to minus 20 degrees. Here, it goes without saying that various heat sources other than steam may be used as the heat source used in the preheater 30.

A standard high pressure compressor (SHP compressor) 40 pressurizes the evaporated gas generated in the liquefied gas storage tank 10 and supplies the pressurized gas to the propulsion engine 50 (customer) And on the line L2 in parallel with each other.

At this time, the standard high-pressure evaporative gas compressor 40 may be provided as the first to fifth evaporative gas compressors 41 to 45 (constituent compressors) and may be provided in parallel with each other on the evaporative gas supply line L2.

Each of the evaporative gas compressors 41-45 in the standard high-pressure evaporative gas compressor 40 can be connected in series with a plurality of stages (pistons) to multi-stage the evaporation gas. For example, the first to fifth evaporative gas compressors 41 to 45 have a structure in which four or five pistons are connected in series, that is, four or five stages in series. In the final stage, To about 350 bar (preferably about 300 bar), and the compressed air can be supplied to the propulsion engine 50. At this time, the fifth evaporative gas compressor 45 may serve as a spare compressor.

The first bypass line BL1 may be branched between the first evaporative gas compressor 41 on the evaporative gas supply line L2 and the propulsion engine 50 and may be supplied upstream of the preheater 30. At this time, a valve (not shown) may be provided at the branching point on the evaporation gas supply line L2, and the valve may be connected to the flow rate of the evaporation gas supplied to the propulsion engine 50 or the evaporation gas supplied to the preheater 30 And it can be a three-way valve.

The first to fifth evaporative gas compressors 41 to 45 may be equipped with evaporative gas coolers (not shown) between their respective stages. When the evaporation gas is pressurized by the first to fifth evaporative gas compressors 41 to 45, the temperature can also be raised 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 fifth evaporative gas compressors 41 to 45 and each evaporative gas cooler is connected to each of the first to fifth evaporative gas compressors 41 to 45 As shown in FIG.

The first to fifth evaporative gas compressors 41 to 45 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 is required at the front ends of the first to fifth evaporative gas compressors 41 to 45, and the preheater 30 is provided in the embodiment of the present invention.

The preheater 30 increases the temperature of the evaporation gas at approximately minus 110 degrees generated in the liquefied gas storage tank 10 from -40 degrees to -20 degrees to the first to fifth evaporative gas compressors 41 to 45 .

Here, the standard high-pressure evaporative gas compressor 40 (SHP compressor) can be formed such that the cylinder is formed in a V-shape so that the size of the compressor itself is considerably reduced, thereby drastically reducing the space occupied by the compressor.

Further, when any one of the standard high-pressure evaporative gas compressors 40 is shut down, for example, when the first evaporative gas compressor 41 is shut down, it is controlled in the standby state under the preset condition, When the predetermined period is exceeded, the first evaporative gas compressor (41) which is in an operation standby state is operated, and the evaporated gas discharged from the first evaporative gas compressor (41), which has been started to operate through the first bypass line (BL1) 30). ≪ / RTI >

The propulsion engine 50 uses evaporative gas or liquefied gas from the liquefied gas storage tank 10 as fuel. At this time, the propulsion engine 50 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 propulsion engine 50 rotates the crankshaft (not shown) connected to the piston, A propeller shaft (not shown) connected to the crankshaft can be rotated. Therefore, as the propeller (not shown) connected to the propeller shaft rotates when the propulsion engine 50 is driven, the ship 100 can advance or reverse.

The propulsion engine 50 is a two-stroke DF engine, typically 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 required for driving the propulsion engine 50. [

In the embodiment of the present invention, the first control valve B1 and the pressure sensor P may be further included.

The first control valve B1 is provided on the first bypass valve BL1 and opens the first bypass valve BL1 to supply at least a part of the evaporated gas discharged from the first evaporative gas compressor 41 to the upstream of the pre- Can be opened and closed. At this time, the first control valve B1 may be connected to the control unit by wire or wireless, and may receive an opening or closing instruction.

The pressure sensor P may be provided inside or outside the liquefied gas storage tank 10 and may be a liquefied gas storage tank 10 which is raised or lowered by evaporation gas generated in the liquefied gas storage tank 10, And transmit the measured internal pressure to the control unit. At this time, the pressure sensor P may be connected to the control unit by wire or wirelessly, of course, and the evaporated gas generation amount may be calculated through the measured internal pressure. (Specifically, the liquefied gas storage It is possible to measure the amount of evaporation gas generated in the liquefied gas storage tank 10 through the property value of the evaporation gas remaining in the tank 10. Therefore, . ≪ / RTI >

The control unit receives the evaporation gas generation amount measured from the pressure sensor (P) and can control driving of the standard high-pressure evaporative gas compressor (40).

Specifically, when the amount of evaporation gas generated from the pressure sensor P is equal to or less than the predetermined amount, the control unit stops the operation of any one of the standard high-pressure evaporative gas compressors 40 (for example, the first evaporative gas compressor 41) And to control the load of the remaining (for example, the second to fourth evaporative gas compressors 42 to 44) of the standard high-pressure evaporative gas compressor 40 connected in parallel.

At this time, the control unit can control the evaporated gas compressor 41, which has been shut down, to be in an operation standby state under the preset condition, and when the operation standby state exceeds the predetermined period, the evaporative gas compressor 41 So that the evaporated gas discharged from the evaporative gas compressor 41 started to operate through the first bypass line BL1 is bypassed to the upstream of the preheater 30. [

That is, the control unit restarts the evaporative gas compressor 41, which is in the operation standby state, when the operation state of the evaporative gas compressor 41 in the operation standby state exceeds the preset period, It is possible to open the opening and control so that the evaporated gas discharged from the evaporative gas compressor 41 in the standby state is bypassed to the upstream of the preheater 30 through the first bypass line BL1.

Alternatively, the control unit may control to stop the evaporative gas compressor 41 that is in standby when the operation standby state exceeds the preset period, but this may be performed as a separate embodiment.

Here, the preset condition is a condition that the evaporation gas compressor 41 is stopped at the time for restarting the operation of the evaporated gas compressor 41 and reaches the time before the evaporation gas compressor 41 is operated. The time point at which the evaporated gas compressor 41 is shut down is the time when the internal pressure of the liquefied gas storage tank 10 exceeds the preset pressure or the evaporated gas generation amount generated in the liquefied gas storage tank 10 is It means that the set generation amount is exceeded.

As described above, in the embodiment of the present invention, when the operation of the standard high-pressure evaporative gas compressor 40 is continued for a long period of time, the evaporative gas is bypassed without stopping operation, The evaporated gas supplied to the standard high pressure evaporative gas compressor 40 is supplied to the standard high pressure evaporative gas compressor 40 by supplying the bypassed evaporated gas to the upstream of the preheater 30, It is possible to increase the driving efficiency of the light source 40 and minimize the construction cost.

The control unit controls whether the standard high-pressure evaporative gas compressor (40) is driven according to the amount of evaporative gas generated in the liquefied gas storage tank (10). If the evaporative gas generation amount is less than the predetermined amount, 40 to stop operation of at least one of them.

At this time, the predetermined generation amount is the amount of evaporated gas flowing into the standard high-pressure evaporative gas compressor 40 from the ineffective point of the standard high-pressure evaporative gas compressor 40, and the ineffective point of the standard high- Is a point at which the power consumption is not reduced even if the flow rate supplied to the standard high-pressure evaporative gas compressor (40) is decreased at the ratio of the flow rate of the flow rate of the refrigerant gas (40)

The load at the inefficiency point of the standard high-pressure evaporative gas compressor 40 may be 20 to 40% of the flow rate at which the standard high-pressure evaporative gas compressor 40 has the maximum load.

Details thereof will be described in detail with reference to FIG.

12 is a graph of power consumption versus flow rate of an evaporative gas compressor according to an embodiment of the present invention. Here, the fifth evaporative gas compressor 45 is not included in the control of the present invention as it is the same compressor or spare compressor as the first to fourth evaporative gas compressors 41 to 44, and is not included in the following description.

As shown in the graph of FIG. 12, the first to fourth evaporative gas compressors 41 to 44 increase the power consumption proportionally as the flow rate increases when the flow rate is the ineffective point (A) or more. 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 41 to 44, the driving conditions, etc., and the first to fourth evaporative gas compressors 41 to 44, 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 41 to 44 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 41 to 44.

That is, a part of the evaporation gas flowing into the first to fourth evaporation gas compressors 41 to 44 is recycled to increase the evaporation gas flow volume to the first to fourth evaporation gas compressors 41 to 44 by a predetermined value or more It is possible to prevent the first to fourth evaporative gas compressors 41 to 44 from surging. At this time, in order to perform recycling, separate power consumption is generated in the first to fourth evaporative gas compressors 41 to 44, and the power is supplied to the first to fourth evaporative gas compressors 41 to 44 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 41 to 44 are driven in parallel, the characteristics of the first to fourth evaporative gas compressors 41 to 44 The power consumed by the first to fourth evaporative gas compressors 41 to 44 can be minimized.

That is, in the embodiment of the present invention, at least one of the first to fourth evaporative gas compressors (41 to 44) is operated when the evaporation gas generation amount is equal to or less than a predetermined value 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) , And the flow rates of the evaporation gas flowing into the first to fourth evaporative gas compressors 41 to 44 are each 30 (when the evaporation gas generation amount generated in the liquefied gas storage tank 10 is equal to or smaller than the predetermined generation amount) The case where both of the first to fourth evaporative gas compressors 41 to 44 are driven and the case where the power consumption when the first evaporative gas compressor 41 of the first to fourth evaporative gas compressors 41 to 44 is standby Let's compare them.

1), all of the first to fourth evaporative gas compressors 41 to 44 are driven, so that the power consumption is 50 * 4 = 200. However, in case 2), the driving of the first evaporative gas compressor 41 is stopped and the evaporative gas is further supplied to the remaining second to fourth evaporative gas compressors 42 to 44 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.

In this embodiment of the present invention, when the first to fourth evaporative gas compressors 41 to 44 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 41 To 44), it is possible to minimize the power consumption of the first to fourth evaporative gas compressors (41 to 44).

In addition, when the evaporation gas generation amount is repeatedly generated below the predetermined generation amount, the control unit may perform at least one of the first to fourth evaporative gas compressors 41 to 44 in an alternate manner in a standby state.

Specifically, the control unit controls at least one of the first to fourth evaporative gas compressors (41 to 44) to be in a standby state when the evaporation gas generation amount is equal to or less than the preset generation amount, , It is possible to control the remaining one of the first to fourth evaporative gas compressors 41 to 44 to be in the standby state.

For example, the control unit controls the first evaporative gas compressor (41) to be in the standby state and the second to fourth evaporative gas compressors (42 to 44) to be in the operating state when the evaporative gas generation amount is less than the preset generation amount .

When the evaporation gas generation amount returns to exceed the preset generation amount, the control unit releases the standby state of the first evaporative gas compressor (41) and restarts the operation so that the first to fourth evaporative gas compressors (41 to 44) Respectively.

Next, when the evaporation gas generation amount changes again to the preset generation amount or less, the second evaporative gas compressor (42) other than the first evaporative gas compressor (41) is controlled to be in an operation stop state and the first, The evaporative gas compressors (41, 43, 44) are controlled to maintain the operating state.

Therefore, in the embodiment of the present invention, the durability of the first to fourth evaporative gas compressors 41 to 44 can be improved by performing the above-described alternate control through the control unit.

In addition, the control unit controls at least one of the first to fourth evaporative gas compressors 41 to 44 to an operation stop state, and controls the operation of the evaporative gas compressor 41, which has been stopped, to an operation standby state under preset conditions.

Here, the control unit may control or stop the operation of the evaporative gas compressor (41) waiting for operation when the standby state of the evaporative gas compressor (for example, the first evaporative gas compressor (51) , It is possible to control the evaporative gas compressor 41 to be operated again and to bypass the evaporative gas discharged from the evaporative gas compressor 41 started to operate through the first bypass line BL1 to the front end of the preheater 30 have.

Of course, each of the second to fourth evaporative gas compressors 42 to 44 may be provided with a bypass line (not shown), and each bypass line is provided with a control valve (not shown) The bypass control may be performed through the valve.

Here, the preset condition may be a condition in which the evaporated gas compressor (41) stops operating at a point in time for restarting the evaporated gas compressor (41) and reaches the time before the evaporated gas compressor (41) is restarted, The time point at which the evaporation gas compressor 41 restarts is a time point when the internal pressure of the liquefied gas storage tank 10 exceeds the preset pressure or when the evaporation gas generation amount generated in the liquefied gas storage tank 10 exceeds the preset generation amount Lt; / RTI >

As described above, in the embodiment of the present invention, the first to fourth evaporative gas compressors 41 to 44 can be returned from the stand-by state or from the operation stop state to the quick operation state through the control unit 90, And the stability is maximized.

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

2, the gas processing system 1 according to the second embodiment of the present invention includes a liquefied gas storage tank 10, a boosting pump 20, a preheater 30, a standard high-pressure evaporative gas compressor 40, a propulsion engine 50, and first and second controllers (not shown).

In the embodiment of the present invention, the configuration except for the standard high-pressure evaporative gas compressor 40 and the first and second control units is the same as that of the first embodiment except that each of the components of the gas processing system 1 according to the first embodiment of the present invention The same reference numerals are used for the sake of convenience in configuration and convenience, but they are not necessarily referred to as the same reference numerals.

Hereinafter, a gas processing system 1 according to a second embodiment of the present invention will be described with reference to FIG. 2, and a standard high pressure evaporative gas compressor 40 and a control unit will be mainly described.

The standard high-pressure evaporative gas compressor 40 is the same as that described in the first embodiment, and there is a difference in that a variable-frequency drive device is constructed in at least some of the compressors as described below.

The standard high-pressure evaporative gas compressor 40 is provided with at least one variable frequency drive (VFD) device among the first to fifth evaporative gas compressors 41 to 45 as constituent compressors, Lt; / RTI >

For example, in the embodiment of the present invention, the first evaporative gas compressor 41, the second evaporative gas compressor 42 may be controlled by a variable frequency drive (VFD), and a fifth evaporative gas compressor 45, The variable frequency drive (VFD) can also be controlled.

 The variable frequency drive control of the standard high-pressure evaporative gas compressor 40 is described in detail in the control section.

In the embodiment of the present invention, a flow sensor F and a pressure sensor P may be further included.

The pressure sensor P may have a first pressure sensor P1 disposed between the propulsion engine 50 and the standard high pressure evaporative gas compressor 40 on the evaporation gas supply line L2, And may have a second pressure sensor P2 installed inside or outside to measure the internal pressure of the liquefied gas storage tank 10, such as the pressure sensor P in one embodiment. Of course, the pressure sensor P may be connected to the control unit by wire or wireless, and the first pressure sensor P1 may be connected to the first control unit and the second pressure sensor P2 may be connected to the second control unit.

The flow sensor F may be disposed between the standard high pressure evaporative gas compressor 40 and the propulsion engine 50 on the evaporative gas supply line L2 and may be disposed between the standard high pressure evaporative gas compressor 40 and the standard high pressure evaporative gas compressor 40, The flow rate can be measured and transmitted to the control unit. At this time, of course, the flow sensor F may be connected to the control unit by wire or wirelessly.

The control unit controls the standard high-pressure evaporative gas compressor 40 according to the pressure or flow rate of the evaporative gas required by the propulsion engine 50 or controls the standard high-pressure evaporative gas compressor 40 according to the amount of evaporative gas generated in the liquefied- (40). Here, the control unit may be divided into a first control unit and a second control unit. Hereinafter, the first and second control units are divided according to the role of the control unit.

The first control unit controls the pressure or the flow rate of the evaporative gas discharged from the plurality of evaporative gas compressors (standard high-pressure evaporative gas compressor (40)) in accordance with the pressure or flow rate of the evaporative gas required by the propulsion engine (50) (Standard high-pressure evaporative gas compressor 40) is controlled by the variable-frequency drive according to the pressure or the flow rate of the evaporation gas required by the engine 50. [

Specifically, the first control unit compares the pressure or flow rate of the evaporation gas requested by the propulsion engine 50 with the pressure measured at the first pressure sensor P1 or the flow rate measured at the flow sensor F, The fourth evaporative gas compressors 41 to 44 can be controlled.

More specifically, when the pressure of the evaporation gas required by the propulsion engine 50 is lower than the pressure measured by the first pressure sensor P1, the first control unit controls the first and second evaporator gas compressors 41 and 42 When the pressure of the evaporation gas required by the propulsion engine 50 is higher than the pressure measured by the first pressure sensor P1, the first and second evaporative gas compressors 41 , 42) of the variable frequency drive.

The second control unit can control the standard high-pressure evaporative gas compressor 40 according to the amount of evaporative gas generated in the liquefied gas storage tank 10.

Specifically, the second control unit controls any one of the standard high-pressure evaporative gas compressors (40) to be in a standby state when the evaporative gas generation amount delivered from the second pressure sensor (P2) is equal to or less than the preset generation amount, The variable frequency drive can be controlled to increase the remaining load.

Herein, the predetermined generation amount is the amount of evaporated gas flowing into the standard high-pressure evaporative gas compressor 40 from the ineffective point of the standard high-pressure evaporative gas compressor 40, and the ineffective point of the standard high-pressure evaporative gas compressor 40 is the standard high- 40), the power consumption is not reduced even if the flow rate supplied to the standard high-pressure evaporative gas compressor (40) decreases.

And the load at the inefficient point of the standard high pressure evaporative gas compressor 40 may be 20 to 40% of the flow rate at which the standard high pressure evaporative gas compressor 40 has the maximum load.

Thus, in the second embodiment of the present invention, the standard high-pressure evaporative gas compressor 40 is controlled through variable frequency drive control without additional construction of a bypass line, a valve or a buffer tank, It is possible to reduce the construction cost and enlarge the use space of the ship 100. In addition,

3 is a conceptual view of a ship including a gas treatment system according to a third embodiment of the present invention.

3, the gas processing system 1 according to the third embodiment of the present invention includes a liquefied gas storage tank 10, a boosting pump 20, a preheater 30, a standard high-pressure evaporative gas compressor 40, a propulsion engine 50, a buffer tank 51, and a control unit (not shown).

In the embodiment of the present invention, configurations except for the buffer tank 51 and the control unit are the same as those in the gas processing system 1 according to the first embodiment of the present invention, However, it is not necessarily the same configuration.

Hereinafter, a gas processing system 1 according to a third embodiment of the present invention will be described with reference to FIG. 3, and the buffer tank 51 and the control unit will be mainly described.

Before describing the buffer tank 51 and the control unit, the second bypass line BL2 and the second control valve B2, which are additionally provided in the embodiment of the present invention, will be described, and the pressure sensor P and the evaporation gas supply Additional description will be made for the line L2.

The second bypass line BL2 branches downstream of the standard high pressure evaporative gas compressor 40 on the evaporative gas supply line L2 and is connected upstream of the standard high pressure evaporative gas compressor 40, B2 so that the evaporated gas supplied from the liquefied gas storage tank 10 and compressed in the standard high pressure evaporative gas compressor 40 is supplied again to the upstream side of the standard high pressure evaporative gas compressor 40.

The second control valve B2 is provided on the second bypass line BL2 and supplies at least a part of the evaporated gas discharged from the first evaporated gas compressor 41 to the upstream of the first evaporated gas compressor 41 It is possible to open and close the opening to supply. At this time, the second control valve B2 may be connected to the control unit by wire or wireless, and may receive an opening or closing instruction.

The pressure sensor P in the embodiment of the present invention may have a first pressure sensor P1 disposed between the propulsion engine 50 and the standard high pressure evaporative gas compressor 40 on the evaporation gas supply line L2 , But also a second pressure sensor P2 installed inside or outside to measure the internal pressure of the liquefied gas storage tank 10 like the pressure sensor P in the first embodiment. Of course, the pressure sensor P may be connected to the control unit by wire or wirelessly.

In the embodiment of the present invention, the evaporation gas supply line L2 may be connected to the first to fifth evaporative gas compressors 41 to 45 in parallel, and the first to fifth evaporative gas compressors 41 to 45 May be referred to as first to fifth supply lines (not shown).

Since the evaporation gas supply lines L2 are formed in common upstream and downstream of the first to fifth supply lines, the upstream of the first to fifth supply lines can be referred to as the upstream common line, and the first to fifth The downstream of the feed line may be referred to as the downstream common line.

The buffer tank 51 is provided between the standard high-pressure evaporative gas compressor 40 and the propulsion engine 50 on the evaporative gas supply line L2 and is connected to the compression compressors of the standard high-pressure evaporative gas compressor 40 at different pressures And supplies the evaporative gases to the propulsion engine 50. The propulsion engine 50 is a propulsion engine.

The buffer tank 51 may be provided downstream of the first to fourth evaporative gas compressors 41 to 44 on the first to fourth supply lines. Alternatively, the buffer tank 51 may be provided solely in the downstream common line.

The control unit controls at least one of the standard high-pressure evaporative gas compressors (40) to a stand-by state in which the operation stop state or the compression of the evaporative gas is not implemented according to the evaporative gas generation amount generated in the liquefied gas storage tank (10) The evaporative gas flow downstream of the standard high-pressure evaporative gas compressor 40 can be controlled according to the amount of evaporative gas generated in the storage tank 10.

Specifically, when the amount of evaporation gas generated in the liquefied gas storage tank 10 is equal to or greater than the predetermined amount, the control unit controls the evaporation gas discharged from the standard high-pressure evaporative gas compressor 40 to flow to the second bypass line BL2 And controls the evaporated gas discharged from the standard high pressure evaporative gas compressor 40 to flow to the buffer tank 51 when the amount of evaporative gas generated in the liquefied gas storage tank 10 is less than the predetermined amount.

Herein, the predetermined generation amount is the amount of evaporated gas flowing into the standard high-pressure evaporative gas compressor 40 from the ineffective point of the standard high-pressure evaporative gas compressor 40, and the ineffective point of the standard high-pressure evaporative gas compressor 40 is the standard high- 40), the power consumption is not reduced even if the flow rate supplied to the standard high-pressure evaporative gas compressor (40) decreases.

And the load at the inefficient point of the standard high pressure evaporative gas compressor 40 may be 20 to 40% of the flow rate at which the standard high pressure evaporative gas compressor 40 has the maximum load.

As described above, in the third embodiment of the present invention, only the buffer tank 51 is constructed without additional construction of a bypass line, a valve, etc., and the fuel to be supplied to the propulsion engine 50 can be stably supplied. And the use space in the ship 100 is enlarged.

In addition, since the stable supply to the propulsion engine 50 is possible with only the buffer tank 51 without complicated control logic, the reliability of the fuel supply is improved and the system stability is maximized.

4 is a conceptual view of a ship including a gas treatment system according to a fourth embodiment of the present invention.

4, the gas processing system 1 according to the fourth embodiment of the present invention includes a liquefied gas storage tank 10, a boosting pump 20, a preheater 30, a standard high pressure evaporative gas compressor 40, a propulsion engine 50, an oil storage tank 60, an oil pump 61, and a control unit (not shown).

In the embodiment of the present invention, configurations other than the oil storage tank 60, the oil pump 61, and the control unit are the same as those of the first embodiment of the gas processing system 1 according to the first embodiment of the present invention The same reference numerals are used for the sake of convenience, but they are not necessarily construed to be the same.

Hereinafter, the gas treatment system 1 according to the fourth embodiment of the present invention will be described with reference to FIG. 4, and the oil storage tank 60, the oil pump 61 and the control unit will be mainly described.

Before describing the oil storage tank 60, the oil pump 61 and the control unit, the oil supply line L3, which is additionally provided in the embodiment of the present invention, will be described.

The embodiment of the present invention may further include an oil supply line L3.

The oil supply line L3 is connected to the oil storage tank 60 and the propulsion engine 50 directly or by connecting the oil storage tank 60 and the evaporation gas supply line L2 to each other, The oil can be supplied to the propulsion engine 60.

The oil supply line L3 may include a valve (not shown) for controlling the supply of oil and an oil pump 61. The oil pump 61 may be connected to the oil supply line L3, You may receive an interruption order.

The pressure sensor P in the embodiment of the present invention can be installed inside or outside to measure the internal pressure of the liquefied gas storage tank 10 like the pressure sensor P in the first embodiment, The sensor P may be connected to the control unit by wire or wirelessly.

The oil storage tank 60 stores oil to be supplied to the propulsion engine 50 and may be directly connected to the propulsion engine 50 through the oil supply line L3 or may be connected to the evaporation gas supply line L2.

The oil storage tank 60 may have the form of a storage tank for storing oil, and the oil may be marine diesel oil (MDO) or heavy oil (HFO).

The oil pump 61 supplies the oil stored in the oil storage tank 60 to the propulsion engine 50 so that the pressure required by the propulsion engine 50 and the pressure of the evaporation gas supplied by the standard high- And supplies the oil to the propulsion engine 50 to compensate for the difference in pressure.

At this time, the oil pump 61 may be provided inside or outside the oil storage tank 60, and may be, for example, a centrifugal pump.

The control unit controls at least one of the standard high-pressure evaporative gas compressors (40) to a stand-by state in which the operation stop state or the compression of the evaporative gas is not implemented according to the evaporative gas generation amount generated in the liquefied gas storage tank (10) The oil pump 61 can be controlled according to the amount of evaporation gas generated in the storage tank 10.

Specifically, when the amount of evaporation gas generated in the liquefied gas storage tank 10 is less than the predetermined amount, the control unit controls the pressure required by the propulsion engine 50 and the pressure of the evaporation gas supplied from the standard high- The oil pump 61 can be controlled to supply the required amount of oil to the propulsion engine 50 by the pressure difference.

The control unit allows the oil to be directly supplied to the propulsion engine 50 through the oil supply line L3 so that the pressure required by the propulsion engine 50 with the pressure generated by burning the oil by the propulsion engine 50, It is possible to control so as to compensate for the difference in the pressure of the evaporated gas supplied by the evaporative gas compressor (40).

Herein, the predetermined generation amount is the amount of evaporated gas flowing into the standard high-pressure evaporative gas compressor 40 from the ineffective point of the standard high-pressure evaporative gas compressor 40, and the ineffective point of the standard high-pressure evaporative gas compressor 40 is the standard high- 40), the power consumption is not reduced even if the flow rate supplied to the standard high-pressure evaporative gas compressor (40) decreases.

And the load at the inefficient point of the standard high pressure evaporative gas compressor 40 may be 20 to 40% of the flow rate at which the standard high pressure evaporative gas compressor 40 has the maximum load.

Thus, in the fourth embodiment of the present invention, only the oil storage tank 60 and the oil pump 61 are constructed without additional construction of the bypass line, the valve, the buffer tank, and the like, It is possible to stably supply the fuel to be supplied to the propulsion engine 50 by compensating the pressure difference due to the pressure fluctuation by the control of the control unit for controlling the supply of the oil to prevent the pressure fluctuation of the evaporation gas discharged from the propulsion engine 50, And the use space in the ship 100 is widened.

5 is a conceptual view of a ship including a gas treatment system according to a fifth embodiment of the present invention.

5, the gas processing system 1 according to the fifth embodiment of the present invention includes a liquefied gas storage tank 10, a boosting pump 20, an additional preheater 31, a standard high-pressure evaporative gas compressor (40), a propulsion engine (50), an evaporative gas heat exchanger (70), and a control unit (not shown).

In the embodiment of the present invention, configurations excluding the additional preheater 31, the evaporation gas heat exchanger 70, and the control unit are the same as those in the first embodiment of the gas processing system 1 according to the first embodiment of the present invention The same reference numerals are used for the sake of convenience in configuration and convenience, but they are not necessarily referred to as the same reference numerals.

Hereinafter, a gas processing system 1 according to a fifth embodiment of the present invention will be described with reference to FIG. 5, and the additional preheater 31, the evaporation gas heat exchanger 70, and the control unit will be mainly described. In the embodiment of the present invention, the standard high-pressure evaporative gas compressor (40) may be referred to as a room-temperature evaporative gas compressor.

Before describing the additional preheater 31, the evaporation gas heat exchanger 70 and the control unit, the refill liquefaction line L5, which is additionally provided in the embodiment of the present invention, will be described.

The reflux line L5 is branched downstream of the standard high pressure evaporative gas compressor 40 on the evaporation gas supply line L2 and is connected to the liquefied gas storage tank 10 and has an evaporation gas heat exchanger 70 . The re-liquefaction line L5 may include a valve (not shown) for controlling the supply of the evaporation gas.

The additional preheater 31 is provided between the evaporation gas heat exchanger 70 on the evaporation gas supply line L2 and the evaporation gas compressor 40 for room temperature and supplies the evaporation gas supplied to the evaporation gas compressor for room temperature 40 And may be operated only when the evaporation gas heat exchanger (70) is not operated in at least one of the plural evaporation gas compressors (40) for room temperature.

The additional preheater 31 can be operated only when the evaporating gas heat exchanger 70 is not operated in any one of the constituent compressors 41 to 44 (for example, the first evaporating gas compressor 41).

The additional preheater 31 is provided with a capacity capable of preheating the amount of evaporative gas that can be processed by one of the room-temperature evaporative gas compressors 40 (one constituent compressor, for example, one of the first evaporative gas compressors 41) Lt; / RTI >

The evaporation gas heat exchanger 70 is provided on the refill lining line L5 and the evaporation gas supply line L2 so that the evaporation gas supplied from the liquefied gas storage tank 10 is supplied to the evaporation gas compressor 40 for room temperature Heat exchange with the compressed evaporated gas.

The evaporated gas heat-exchanged in the evaporative gas heat exchanger 70 includes the evaporated gas compressed in the first to fourth evaporative gas compressors 41 to 44 and the evaporated gas supplied in the liquefied gas storage tank 10, The evaporated gas supplied from the liquefied gas storage tank 10 through heat exchange is heated and the evaporated gas compressed in the first to fourth evaporative gas compressors 41 to 44 is cooled.

The evaporated gas compressed in the first to fourth evaporative gas compressors 41 to 44 among the evaporated gases heat-exchanged in the evaporative gas heat exchanger 70 is supplied to the liquefied gas storage tank 10 and is supplied to the evaporation 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 41 to 44 may be supplied to the first to fourth evaporative gas compressors 41 to 44.

Accordingly, the evaporated gas compressed by the first to fourth evaporative gas compressors 41 to 44 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 41 to 44 is supplied with the heat source from the evaporated gas compressed by the first to fourth evaporative gas compressors 41 to 44 and supplied to the first to fourth evaporative gas compressors 41 to 44, .

The control unit may control the evaporating gas heat exchanger 70 and the additional preheater 31 depending on whether or not the evaporated gas compressed in the evaporation gas compressor 40 for room temperature is supplied to the evaporation gas heat exchanger 70.

Specifically, when the evaporated gas compressed in the room-temperature evaporative gas compressor 40 is not supplied to the evaporative gas heat exchanger 70, the control unit activates the additional pre-heater 31 and the evaporative gas compressor 40 When the compressed evaporated gas is supplied to the evaporation gas heat exchanger 70, it is possible to control the operation of the additional preheater 31 to be stopped. When the evaporation gas heat exchanger 70 is not in operation (when the evaporation gas compressed in the room-temperature evaporation gas compressor 40 is not supplied to the evaporation gas heat exchanger 70), the evaporation gas heat exchanger 70, (In the case where the evaporation gas compressed in the room-temperature evaporation gas compressor 40 is supplied to the evaporation gas heat exchanger 70).

The control of the control unit may be performed in the initial driving period of the evaporative gas heat exchanger 70 before the evaporative gas heat exchanger 70 is driven.

There is a period during which the evaporation gas heat exchanger 70 is not supplied with the evaporation gas compressed by the room-temperature evaporation gas compressor 40 for a while. In this case, there is a fear that the evaporation gas which is not preheated to the room-temperature evaporation gas compressor 40 is supplied, and the initial driving efficiency of the room-temperature evaporation gas compressor 40 is very low.

In the embodiment of the present invention, the preheater 30 is not provided and the additional preheater 31 is provided only upstream of the first evaporative gas compressor 41, and then the initial stage of the evaporator gas heat exchanger 70 Only the first evaporative gas compressor 41 can be controlled to be driven only during the driving period.

The evaporated gas heat exchanger 70 is supplied with the evaporated gas compressed in the first evaporated gas compressor 41 in the initial driving period of the evaporated gas heat exchanger 70 so as to be heat exchanged in the evaporated gas heat exchanger 70 And the preheated evaporated gas can be supplied to the remaining second to fourth evaporative gas compressors 42 to 44.

That is, in the embodiment of the present invention, the driving efficiency of the room-temperature evaporative gas compressor 40 can be optimized through the control of the controller as described above to maximize the driving efficiency, and the first to fourth evaporative gas compressors 41 to 44 The first preheater 31 having a capacity capable of covering the flow rate of the evaporation gas introduced into the first evaporative gas compressor 41 can be used instead of the preheater having a large capacity capable of covering the flow rate of the evaporation gas introduced into the first evaporation gas compressor 41, It is possible to optimize the preheating of the evaporated gas supplied to the fourth evaporative gas compressors 41 to 44 so that the construction cost is reduced and the space utilization is maximized.

In the embodiment of the present invention, it may further include an evaporation gas decompressor (not shown) and a gas-liquid separator (not shown).

The evaporation gas decompressor is provided downstream of the evaporation gas heat exchanger 70 on the re-liquefaction line L5 and is pressurized by the first to fourth evaporative gas compressors 41 to 44 to perform heat exchange in the evaporation gas heat exchanger 70 And at least a part of the evaporated gas is liquefied. For example, the evaporation gas decompressor 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 cooling effect can be achieved.

In this embodiment, the evaporated gas pressurized by the first to fourth evaporative gas compressors 41 to 44 is heat-exchanged with the evaporated gas supplied from the liquefied gas storage tank 10 in the evaporated gas heat exchanger 70, The pressure can maintain the discharge pressure discharged from the first to fourth evaporative gas compressors (41 to 44).

Accordingly, in the present embodiment, it can be said that the high pressure is maintained even after the evaporated gas pressurized by the first to fourth evaporative gas compressors 41 to 44 is heat-exchanged in the evaporative gas heat exchanger 70 and supplied with cold heat So that the evaporation gas is reduced through the evaporation gas decompressor so that the evaporation gas is further cooled.

Accordingly, the evaporated gas pressurized in the first to fourth evaporative gas compressors 41 to 44 is partially re-liquefied in the evaporative gas heat exchanger 70, but can finally be completely liquefied in the evaporative gas decompressor.

Specifically, the evaporation gas may be multi-stage pressurized by the first to fourth evaporative gas compressors 41 to 44 to have a pressure of 150 to 350 bar, and the temperature may be about 45 degrees. The evaporated gas raised to a temperature of about 45 degrees is recovered by the evaporation gas heat exchanger 70 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 evaporation gas decompressor. At this time, the evaporation gas in the evaporation gas decompressor is cooled by the decompression, 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, 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 evaporative gas pressure reducer may be a Joule-Thomson valve. Alternatively, the evaporative gas decompressor may consist of an expander (expander).

The inflator can be driven without using any additional power. Particularly, the efficiency of the gas processing system 1 can be improved by utilizing the generated power as electric power for driving the first to fourth evaporative gas compressors 41 to 44. The power transmission may be accomplished by, for example, a gear connection or an electric conversion and the like.

The gas-liquid separator is provided downstream of the evaporation gas decompressor provided downstream of the evaporation gas heat exchanger 70 on the re-liquefaction line L5, temporarily stores the decompressed or expanded evaporation gas in the evaporation gas decompressor, The gravity separates the evaporative gas into liquid and gas.

At this time, the gas is flash gas, and the temperature is approximately -162.3 degrees. This 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 70 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 70 at a temperature of -110 to -120 degrees (-114 degrees).

Therefore, the 45-degree evaporation gas recovered along the reflux line L5 is cooled by heat exchange with the mixed gas of -110 to -120 degrees supplied through the evaporation gas supply line L2 in the evaporation gas heat exchanger 70 . 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).

Accordingly, the evaporation gas discharged from the evaporation gas heat exchanger 70 and flowing into the evaporation gas decompressor may be about -112 degrees lower than the case where there is no flash gas circulation (about -97 degrees), and the decompression gas It can be cooled to about -163.7 degrees. In this case, more evaporative gas can be liquefied by the evaporative gas decompressor and recovered to the liquefied gas storage tank 10 than when the flash gas is not circulated.

Therefore, in this embodiment, by supplying the flash gas generated through the gas-liquid separator to the upstream side of the evaporation gas heat exchanger 70, the temperature of the evaporation gas supplied from the liquefied gas storage tank 10 to the evaporation gas heat exchanger 70 becomes So that the liquefaction efficiency of the evaporated gas compressed by the first to fourth evaporative gas compressors 41 to 44 and returned to the evaporative gas heat exchanger 70 can be increased to 60% or more.

In the gas-liquid separator, the evaporation 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 can be recovered as flash gas upstream of the first to fourth evaporative gas compressors 41 to 44 have.

That is, when the evaporation gas is separated into the liquid and the gas in the gas-liquid separator, the liquefied evaporated gas (liquid) and the flash gas (gas) are respectively returned to the liquefied gas storage tank 10 through the re- Can be recovered upstream of the evaporative gas heat exchanger 70 through a flash gas supply line (not shown).

As described above, the gas-liquid separator in this embodiment recovers the liquefied evaporated gas to the liquefied gas storage tank 10 and recovers the flash gas generated in the gas-liquid separator to the upstream of the evaporated gas heat exchanger 70, The gas can be re-liquefied and re-stored in the liquefied gas storage tank 10 and re-pressurized through the first to fourth evaporative gas compressors 41 to 44 without discarding the flash gas to be reused in the propulsion engine 50 have.

6 is a conceptual view of a ship including a gas treatment system according to a sixth embodiment of the present invention.

6, the gas processing system 1 according to the sixth embodiment of the present invention includes a liquefied gas storage tank 10, a boosting pump 20, a high-pressure pump 22, a vaporizer 23, A preheater 30, a standard high-pressure evaporative gas compressor 40, a propulsion engine 50, and a control unit (not shown).

In the embodiment of the present invention, configurations other than the high-pressure pump 22, the vaporizer 23, and the control unit are the same as those of the gas processing system 1 according to the first embodiment of the present invention, The same reference numerals are used, but they are not necessarily denoted by the same reference numerals.

Hereinafter, a gas processing system 1 according to a sixth embodiment of the present invention will be described with reference to FIG. 6, and the high pressure pump 22, the vaporizer 23, and the control unit will be mainly described.

Before describing the high-pressure pump 22, the vaporizer 23, and the control unit, the liquefied gas supply line L4, which is additionally provided in the embodiment of the present invention, will be described.

The liquefied gas supply line L4 is connected to the liquefied gas storage tank 10 and the propulsion engine 50 or to the standard high pressure evaporative gas compressor 40 on the liquefied gas storage tank 10 and the evaporation gas supply line L2, And may include a high-pressure pump 22 and a vaporizer 23. Here, the liquefied gas supply line L4 may include a valve (not shown) for controlling the supply of the liquefied gas.

The high pressure pump 22 is provided between the booster pump 20 and the vaporizer 23 on the liquefied gas supply line L4 and is supplied with the liquefied gas pressurized from the boosting pump 20 and pressurized to a high pressure.

The vaporizer 23 is provided between the high-pressure pump 22 and the propulsion engine 50 on the liquefied gas supply line L4 and supplies the liquefied gas pressurized at a high pressure from the high-pressure pump 22 to vaporize it.

The control unit may control the standard high pressure evaporative gas compressor 40 according to the amount of evaporative gas generated in the liquefied gas storage tank 10 and may evaporate at least one of the standard high pressure evaporative gas compressors 40 according to the evaporative gas generation amount, It can be controlled in a standby state in which gas compression is not implemented.

Specifically, when the evaporation gas generation amount is equal to or less than the predetermined generation amount, the control unit controls either one of the standard high-pressure evaporative gas compressors 40 to be in a standby state and increases the remaining load of the standard high-pressure evaporative gas compressor 40 connected in parallel Can be controlled.

At this time, the predetermined generation amount is the amount of evaporated gas flowing into the standard high-pressure evaporative gas compressor 40 from the ineffective point of the standard high-pressure evaporative gas compressor 40, and the ineffective point of the standard high- Is a point at which the power consumption is not reduced even if the flow rate supplied to the standard high-pressure evaporative gas compressor (40) is decreased at the ratio of the flow rate of the flow rate of the refrigerant gas (40)

The load at the inefficiency point of the standard high-pressure evaporative gas compressor 40 may be 20 to 40% of the flow rate at which the standard high-pressure evaporative gas compressor 40 has the maximum load.

As described above, in the sixth embodiment of the present invention, the load of the standard high-pressure evaporative gas compressor 40 for processing the evaporative gas can be reduced, and the construction cost can be reduced.

7 is a conceptual view of a ship including a gas processing system according to a seventh embodiment of the present invention.

7, the gas processing system 1 according to the seventh embodiment of the present invention includes a liquefied gas storage tank 10, a boosting pump 20, a high-pressure pump 22, a vaporizer 23, A preheater 30, a standard high-pressure evaporative gas compressor 40 (hereinafter may be referred to as a room-temperature evaporative gas compressor), a cryogenic evaporative gas compressor 40a, a propulsion engine 50, a power generation engine 50a, ).

In the embodiment of the present invention, the configurations except for the cryogenic evaporating gas compressor 40a, the power generation engine 50a and the control section are the same as those in the gas processing system 1 according to the first embodiment of the present invention The same reference numerals are used for the sake of convenience in configuration and convenience, but they are not necessarily referred to as the same reference numerals.

Hereinafter, a gas processing system 1 according to a seventh embodiment of the present invention will be described with reference to FIG. 7, and a cryogenic evaporation gas compressor 40a, a power generation engine 50a, and a control unit will be mainly described.

Before describing the cryogenic evaporation gas compressor 40a, the power generation engine 50a, and the control unit, the power generation engine fuel supply line L2a, which is additionally provided in the embodiment of the present invention, will be described.

The power generation engine fuel supply line L2a is connected between the liquefied gas storage tank 10 and the power generation engine 50a or between the preheater 30 on the evaporation gas supply line L2 and the liquefied gas storage tank 10, And connected to the power generation engine 50a, and may have a cryogenic evaporative gas compressor 40a.

The power generation engine fuel supply line L2a can supply the evaporative gas generated in the liquefied gas storage tank 10 to the power generation engine 50a and compress the unheated evaporative gas using the cryogenic evaporative gas compressor 40a And then supplied to the power generation engine 50a.

Here, the power generation engine fuel supply line L2a may have a valve (not shown) for controlling the supply of the evaporation gas, and when the evaporation gas supply line L2 is referred to as the evaporation gas first supply line, Gas second supply line.

The cryogenic evaporation gas compressor 40a pressurizes the evaporated gas supplied from the liquefied gas storage tank 10 branched from the upstream of the preheater 30 and supplies it to the power generation engine 50a.

The cryogenic evaporation gas compressor 40a is provided on the power generation engine fuel supply line L2a and can supply and compress the evaporated gas generated in the liquefied gas storage tank 10 without preheating, (50a).

The power generation engine 50a uses the evaporation gas supplied from the liquefied gas storage tank 10 as fuel. That is, the power generation engine 50a requires evaporative gas and can be driven using the power as the raw material. The power generation engine 50a may be, for example, DFDE or DFDG as a generator, but is not limited thereto.

Specifically, the power generation engine 50a may be connected to the cryogenic evaporating gas compressor 40a through the power generation engine fuel supply line L2a and may be connected to the cryogenic evaporating gas compressor 40a at a low pressure (2 to 8 bar; preferably 4 To 6 bar) to be used as fuel.

In addition, the power generation engine 50a can be a heterogeneous fuel engine in which a heterogeneous fuel can be used, so that it is possible to use not only evaporation gas but also oil as fuel, but a mixture of evaporation gas and oil is not supplied, Can be supplied. This is to prevent the mixture of two materials having different combustion temperatures from being mixed, thereby preventing the efficiency of the power generation engine 50a from deteriorating.

In addition, the power generation engine 50a can generate steam by heating fresh water as a boiler, and generate steam using the generated steam, or store the remaining steam in a separate steam storage medium.

The power generation engine 50a can supply the generated steam to the preheater 30, the additional preheater 31 or the forced vaporizer 21 through which the preheater 30, the additional preheater 31 or the forced vaporizer 21, Allows the evaporation gas to be heated.

At this time, the power generation engine 50a may be referred to as a low pressure consumer when the propulsion engine 50 is referred to as a high pressure consumer.

The control unit can control the standard high pressure evaporative gas compressor 40 (room temperature evaporative gas compressor) according to the amount of evaporative gas generated in the liquefied gas storage tank 10 and can control the standard high pressure evaporative gas compressor 40 Can be controlled to a standby state in which the compression of the evaporative gas is not implemented.

Specifically, when the evaporation gas generation amount is equal to or less than the predetermined generation amount, the control unit controls either one of the standard high-pressure evaporative gas compressors 40 to be in a standby state and increases the remaining load of the standard high-pressure evaporative gas compressor 40 connected in parallel Can be controlled.

At this time, the predetermined generation amount is the amount of evaporated gas flowing into the standard high-pressure evaporative gas compressor 40 from the ineffective point of the standard high-pressure evaporative gas compressor 40, and the ineffective point of the standard high- Is a point at which the power consumption is not reduced even if the flow rate supplied to the standard high-pressure evaporative gas compressor (40) is decreased at the ratio of the flow rate of the flow rate of the refrigerant gas (40)

The load at the inefficiency point of the standard high-pressure evaporative gas compressor 40 may be 20 to 40% of the flow rate at which the standard high-pressure evaporative gas compressor 40 has the maximum load.

As described above, in the seventh embodiment of the present invention, the characteristics of the cryogenic evaporative gas compressor 40a that can be used without the preheater 30 when the room-temperature evaporative gas compressor 40 and the cryogenic evaporative gas compressor 40a are used together It is possible to optimize the energy for processing the evaporative gas and to increase the system efficiency by designing the evaporative gas branched at the upstream of the preheater 30 to be supplied to the cryogenic evaporative gas compressor 40a using the system And the construction cost is reduced.

8 is a conceptual view of a ship including a gas treatment system according to an eighth embodiment of the present invention.

8, the gas processing system 1 according to the eighth embodiment of the present invention includes a liquefied gas storage tank 10, a boosting pump 20, a preheater 30, a standard high-pressure evaporative gas compressor 40, a propulsion engine 50, first to fourth block valves 81 to 84, and a control unit (not shown).

In the embodiment of the present invention, the configurations excluding the first to fourth block valves 81 to 84 and the control section are the same as those in the gas processing system 1 according to the first embodiment of the present invention The same reference numerals are used for the sake of convenience, but they are not necessarily construed to be the same.

Hereinafter, a gas processing system 1 according to an eighth embodiment of the present invention will be described with reference to FIG. 8, and first to fourth block valves 81 to 84 and a control unit will be mainly described.

The first to fourth block valves 81 to 84 are provided downstream of each of the first to fourth evaporative gas compressors 41 to 44 on the evaporative gas supply line L2, It is possible to control the flow rate of the evaporative gas discharged from the evaporator 41 to 44 to the propulsion engine 50.

The first to fourth block valves 81 to 84 may be referred to as first to fourth control valves, and each of the valves may be connected to the control unit through a wire or wireless connection to transmit an opening opening signal or an opening closing signal And can be driven.

The control unit controls at least one of the standard high-pressure evaporative gas compressor (40) in a standby state in accordance with the amount of evaporation gas generated in the liquefied gas storage tank (10) And a second control unit.

The first control unit controls the start of driving of the standard high-pressure evaporative gas compressor (40) (a plurality of evaporative gas compressors), and at the start of operation of the standard high-pressure evaporative gas compressor (40) .

Specifically, when the processing flow rate of the evaporative gas compressor which is first driven in the standard high-pressure evaporative gas compressor (40) becomes equal to or higher than a predetermined flow rate, the first control section controls the evaporative gas compressor can do.

For example, the first evaporative gas compressor to be firstly driven may be referred to as a first evaporative gas compressor 41, the evaporative gas compressor driven next to the first evaporative gas compressor 41 may be referred to as a second evaporative gas compressor 42, The third evaporative gas compressor 43 and the fourth evaporative gas compressor 44 may be the evaporative gas compressors driven continuously.

More specifically, the first control unit closes all of the first to fourth control valves 81 to 84 at the start of driving of the first evaporative gas compressor 41, and the evaporative gas processing flow rate of the first evaporative gas compressor 81 When the predetermined flow rate is reached, the second evaporative gas compressor 42 is started to be driven. When the evaporative gas processing flow rate of the first evaporative gas compressor 41 reaches the maximum operating flow rate, the first control valve 81 is opened Pressure evaporation gas required by the propulsion engine 50 can be supplied to the propulsion engine 50. [ Of course, since the second to fourth control valves 82 to 84 are closed, only the evaporated gas compressed by the first evaporative gas compressor 41 is supplied to the propulsion engine 50.

Subsequently, when the evaporation gas processing flow rate of the second evaporative gas compressor 42 reaches the predetermined flow rate, the evaporative gas processing flow rate of the second evaporative gas compressor 42 starts to be driven to the maximum The first and second evaporative gas compressors 41 and 42 are controlled to open the second control valve 83 so that the high pressure evaporated gas compressed at the pressure required by the propulsion engine 50 is supplied to the propulsion engine 50). (The third and fourth control valves 83 and 84 are still in the closed state).

Next, when the evaporation gas processing flow rate of the third evaporative gas compressor 43 reaches a preset flow rate, the fourth evaporative gas compressor 44 is started to be driven, and the evaporative gas processing flow rate of the third evaporative gas compressor 43 is set to the maximum The third control valve 83 is opened so that the high-pressure evaporation gas compressed by the first to third evaporative gas compressors 41 to 43 to the pressure required by the propulsion engine 50 is supplied to the propulsion engine 50).

The fourth control valve 84 is opened and the first to fourth evaporative gas compressors 41 to 44 drive the propulsion engine 50. When the evaporation gas processing flow rate of the fourth evaporative gas compressor 44 reaches the maximum drive flow rate, It is possible to supply the propelling engine 50 with the required high-pressure evaporating gas.

Here, the predetermined flow rate may be a flow rate of 85 to 95% of the maximum operating flow rate of the standard high-pressure evaporative gas compressor 40.

Through the control of the first control unit, the pressure of the evaporative gas to be supplied to the propulsion engine 50 can be constantly supplied at a high pressure required by the propulsion engine 50, so that the propulsion engine 50 can supply the flexible fuel The stability of the gas processing system 1 is increased, and the driving efficiency of the propulsion engine 50 is maximized.

The second control unit can control the standard high pressure evaporative gas compressor 40 (room temperature evaporative gas compressor) according to the amount of evaporative gas generated in the liquefied gas storage tank 10, and can control the standard high pressure evaporative gas compressor (40) can be controlled to a standby state in which evaporation gas compression is not implemented.

Specifically, the second control unit controls one of the standard high-pressure evaporative gas compressors 40 to be in the standby state when the evaporative gas generation amount is equal to or smaller than the pre-set generation amount, and increases the remaining load of the standard high-pressure evaporative gas compressor 40 connected in parallel .

At this time, the predetermined generation amount is the amount of evaporated gas flowing into the standard high-pressure evaporative gas compressor 40 from the ineffective point of the standard high-pressure evaporative gas compressor 40, and the ineffective point of the standard high- Is a point at which the power consumption is not reduced even if the flow rate supplied to the standard high-pressure evaporative gas compressor (40) is decreased at the ratio of the flow rate of the flow rate of the refrigerant gas (40)

The load at the inefficiency point of the standard high-pressure evaporative gas compressor 40 may be 20 to 40% of the flow rate at which the standard high-pressure evaporative gas compressor 40 has the maximum load.

9 is a conceptual view of a ship including a gas processing system according to a ninth embodiment of the present invention.

9, the gas processing system 1 according to the ninth embodiment of the present invention includes a liquefied gas storage tank 10, a boosting pump 20, a preheater 30, a standard high-pressure evaporative gas compressor 40, a propulsion engine 50, a power generation engine 50a, and a control unit (not shown).

In the embodiment of the present invention, the configurations except for the control unit are the same as those in the gas processing system 1 according to the seventh embodiment of the present invention described with reference to FIG. 7, It does not refer to it.

Hereinafter, a gas processing system 1 according to a ninth embodiment of the present invention will be described with reference to FIG. 9, and the control unit will be mainly described.

Hereinafter, the third bypass line BL3 further included in the embodiment of the present invention will be described before describing the control unit.

The third bypass line BL3 is branched from the middle stage (between the second stage and the third stage) of each of the standard high-pressure evaporative gas compressors 40 provided on the evaporation gas supply line L2, 50a.

The third bypass line BL3 can supply the low-pressure evaporation gas compressed at the second-stage to the third-stage of each of the standard high-pressure evaporation-gas compressors 40 to the power generation engine 50a, And a valve (not shown) for controlling the supply of the gas. Here, when the evaporation gas supply line L2 is referred to as a high-pressure evaporation gas supply line, the third bypass line BL3 may be referred to as a low-pressure evaporation gas supply line.

The control unit controls the standard high-pressure evaporative gas compressor (40) according to whether the ship (100) is navigated or not.

Specifically, the control unit controls the supply of at least one of the standard high-pressure evaporative gas compressors 40 only to the power generation engine 50a when the ship 100 is a ballast voyage, It is possible to control the gas compressor to supply both the power generation engine 50a and the propulsion engine 50. [

At this time, the control unit determines that the amount of evaporative gas supplied to the power generation engine 50a among the evaporative gases compressed in the remaining evaporative gas compressors of the standard high-pressure evaporative gas compressor 40 is greater than the amount of evaporative gas supplied to the propulsion engine 50 Can be controlled to be small.

For example, the control unit controls the evaporative gas compressed in the first and second evaporative gas compressors 41 and 42 to be supplied only to the power generation engine 50a, and compresses the compressed gas in the third and fourth evaporative gas compressors 43 and 44 To supply both the propulsion engine 50 and the power generation engine 50a with the evaporated gas.

At this time, the control unit supplies the value of 200 as the evaporation gas supply flow rate of the first and second evaporative gas compressors 41 and 42 to the power generation engine 50a and controls the propulsion engine 50 not to supply the evaporation gas at all And supply the value of 200 to the power generation engine 50a and supply the value of 700 to the propulsion engine 50 as the evaporation gas supply flow rate of the third and fourth evaporative gas compressors 43 and 44. [

As described above, in the ninth embodiment of the present invention, the evaporation gas can be efficiently treated at the time of the ballast navigation with a small amount of evaporation gas generated, so that consumption of the evaporation gas is optimized, thereby preventing environmental pollution and increasing the system driving efficiency There is an effect.

10 is a conceptual view of a ship including a gas treatment system according to a tenth embodiment of the present invention.

10, the gas processing system 1 according to the tenth embodiment of the present invention includes a liquefied gas storage tank 10, a boosting pump 20, a preheater 30, a standard high-pressure evaporative gas compressor 40, a propulsion engine 50, and a control unit (not shown).

In the embodiment of the present invention, except for the control unit, the same reference numerals are used for the respective constructions in the gas processing system 1 according to the first embodiment of the present invention described with reference to FIG. 1, It does not refer to it.

Hereinafter, a gas processing system 1 according to a tenth embodiment of the present invention will be described with reference to FIG. 10, and the control unit will be mainly described.

The embodiment of the present invention may further include a load sensor (L).

The load sensor L may be provided inside or outside the propulsion engine 50 and may measure the load or the load of the propulsion engine 50 and transmit the measured load to the control unit. At this time, of course, the load sensor L may be connected to the control unit by wire or wirelessly.

The control unit controls the standard high pressure evaporative gas compressor 40 in accordance with the load of the propulsion engine 50 so that at least one of the standard high pressure evaporative gas compressors 40 is compressed according to the load of the propulsion engine 50 Control is performed in a standby state that is not implemented.

Specifically, the control unit receives the load amount of the propulsion engine 50 measured from the load sensor L, and controls the driving of the standard high-pressure evaporative gas compressor 40. The load amount received from the load sensor L is preset It is possible to control any one of the standard high-pressure evaporative gas compressors 40 to be in a standby state and increase the load of the rest of the standard high-pressure evaporative gas compressors 40 connected in parallel when the load is not more than the load amount.

At this time, the predetermined generation amount is the amount of evaporated gas flowing into the standard high-pressure evaporative gas compressor 40 from the ineffective point of the standard high-pressure evaporative gas compressor 40, and the ineffective point of the standard high- Is a point at which the power consumption is not reduced even if the flow rate supplied to the standard high-pressure evaporative gas compressor (40) is decreased at the ratio of the flow rate of the flow rate of the refrigerant gas (40)

The load at the inefficiency point of the standard high-pressure evaporative gas compressor 40 may be 20 to 40% of the flow rate at which the standard high-pressure evaporative gas compressor 40 has the maximum load.

As described above, in the tenth embodiment of the present invention, the standard high-pressure evaporative gas compressor 40 can be driven differentially according to the load of the propulsion engine 50, so that the evaporative gas can be processed very efficiently, Since the load of the compressor 40 can be optimized, consumption of the evaporation gas is optimized, thereby preventing environmental pollution and increasing the system driving efficiency.

11 is a conceptual view of a ship including a gas processing system according to an eleventh embodiment of the present invention.

11, the gas processing system 1 according to the eleventh embodiment of the present invention includes a liquefied gas storage tank 10, a boosting pump 20, a preheater 30, a standard high-pressure evaporative gas compressor 40, the propulsion engine 50, the power generation engine 50a, the gas combustion device 50b, the refueling device 90, the pressure reducing valve 91, the first and second oil separators 92, (Not shown).

In the embodiment of the present invention, configurations excluding the gas combustion device 50b, the refueling device 90, the pressure reducing valve 91, the first and second oil separators 92 and 93, The same reference numerals are used for the respective constructions in the gas processing system 1 according to the seventh embodiment of the present invention, but they are not necessarily referred to the same constructions.

Hereinafter, a gas processing system 1 according to an eleventh embodiment of the present invention will be described with reference to FIG. 11, and a gas combustion device 50b, a remelting device 90, a pressure reducing valve 91, And the second oil separators 92 and 93 and the control unit will be mainly described.

In addition, the standard high-pressure evaporative gas compressor 40 may be a compressor using lubrication oil by implementing the lubrication of the lubrication system in the present embodiment, mixing the lubrication oil with the evaporation gas and compressing the same, 50a and the gas combustion device 50b. (Of course, the supply to the power generation engine 50a and the gas combustion device 50b includes supply to the pressure reducing valve 91).

Before describing the control section, the power generation engine fuel supply line L5a and the gas combustion apparatus fuel supply line L5b, which are additionally provided in the embodiment of the present invention, will be described. Here, unlike in the fifth embodiment, the refueling line L5 is branched from the power generation engine fuel supply line L5a and the gasification unit fuel supply line L5b, and on the refueling line L5, the evaporation gas heat exchanger 70 The regeneration device 90, the pressure reducing valve 91, and the first and second oil separators 92 and 93 may be provided.

The power generation engine fuel supply line L5a may be branched on the redistribution line L5 upstream of the redistribution device 90 and connected to the power generation engine 50a and the gas combustion device fuel supply line L5b may be connected May be branched on the liquefaction line (L5) upstream of the refueling device (90) and connected to the gas combustion device (50b).

At this time, a valve (not shown) for controlling the supply of the evaporation gas may be provided on each line of the power generation engine fuel supply line L5a and the gas combustion apparatus fuel supply line L5b, wherein the evaporation gas supply line L2 The re-liquefaction line L5, the power generation engine fuel supply line L5a, and the gas combustion unit fuel supply line L5b may be referred to as a low-pressure evaporation gas supply line when they are referred to as a high-pressure evaporation gas supply line, The power generation engine fuel supply line L5a may be referred to as a first low-pressure evaporation gas supply line and the gas-fired device fuel supply line L5b may be referred to as a second low-pressure evaporation gas supply line.

The gas combustion unit 50b is connected to the gas combustion unit fuel supply line L5b to supply and discharge the evaporated gas reduced in pressure by the reduced pressure valve 91 and discharge the burnt evaporated gas to the outside .

The gas combustion device 50b may be supplied with a low-pressure evaporation gas as in the power generation engine 50a, and may be burnt by supplying the evaporation gas mixed with the lubricating oil.

Here, the gas combustion device 50b may be referred to as a low-pressure consumer, such as the power generation engine 50a, when the propulsion engine 50 is referred to as a high-pressure consumer, and more specifically, It can be classified and classified as a customer.

The re-liquefier 90 is provided on the re-liquefaction line L5 to supply the evaporated gas depressurized by the depressurizing valve 91 to re-liquefy and supply the re-liquefied evaporated gas to the liquefied gas storage tank 10 .

The remelting device 90 may have a separate refrigerant cycle and may have a refrigerant cycle using nitrogen, for example.

Since the re-liquefier 90 can not use the evaporated gas mixed with the lubricating oil unlike the power generation engine 50a and the gas combustion apparatus 50b, the lubricating oil is supplied by the first and second oil separators 92 and 93 A separate evaporation gas can be supplied.

The re-liquefier 90 may further include a gas-liquid separator (not shown) on the downstream side so as to supply the evaporated gas that has not been liquefied to another evaporative gas consuming place (for example, the gas combustion device 50b or the like). It is possible to prevent the internal pressure of the liquefied gas storage tank 10 from rising sharply.

Here, the refueling device 90 may be referred to as a low-pressure consumer, such as the power generation engine 50a and the gas combustion device 50b when the propulsion engine 50 is referred to as a high-pressure consumer, 50a and the gas combustion device 50b are referred to as a first low-pressure consumer, they may be subdivided into a second low-pressure consumer.

The pressure reducing valve 91 is provided upstream of the branch point of the power generation engine fuel supply line L5a and the gas combustion apparatus fuel supply line L5b on the re-liquefaction line L5, It is possible to reduce at least a part of the evaporation gas supplied from the power generation engine 50a and the gas combustion apparatus 50b to a pressure required by the power generation engine 50a and the gas combustion apparatus 50b. Here, the pressure reducing valve 91 may be referred to as a pressure reducing device.

The pressure reducing valve 91 is, for example, supplied with evaporative gas compressed to 200 to 400 bar by the standard high pressure evaporative gas compressor 40

The first and second oil separators 92 and 93 are provided downstream of the pressure reducing valve 91 on the re-liquefaction line L5 and include lube oil mixed with the evaporation gas reduced in pressure by the pressure reducing valve 91, And the evaporated gas from which the lubricating oil has been separated can be supplied to the refueling device 90. [

That is, since the first and second oil separators 92 and 93 are supplied with the evaporated gas reduced in pressure by the reduced pressure valve 91, the lubricant is separated from the evaporated gas before the reduced pressure by the reduced pressure valve 91 It is possible to remove the lubricating oil by removing the lubricating oil from the evaporating gas before the pressure reducing valve 91 before the pressure reducing valve 91 is removed.

Specifically, the first oil separator 92 is disposed between the upstream of the point where the power generation engine fuel supply line L5a and the gas combustion unit fuel supply line L5b are branched on the remanufacturing line L5 and the pressure reducing valve 91 And the primary lubricating oil removal can be performed on the evaporated gas decompressed in the pressure reducing valve 91.

The first oil separator 92 separates the evaporated gas from which the lubricating oil has been separated into the power generation engine 50a through the power generation engine fuel supply line L5a and the gas combustion apparatus 50b through the gas combustion unit fuel supply line L5b, .

The second oil separator 93 is provided between the downstream of the point where the power generation engine fuel supply line L5a and the gas combustion unit fuel supply line L5b branch on the remanufacturing line L5 and the remanufacturing device 90 And the primary lubricant removed from the primary oil separator 92 can be subjected to secondary lubricant removal.

The second oil separator 93 can safely supply the evaporated gas from which the lubricant is finally removed to the re-liquefier 90, thereby maximizing the driving efficiency of the re-liquefier 90 and maximizing the safety.

That is, the second oil separator 93 is provided in the first oil separator 92 in a complementary manner, so that the lubricant which can not be separated due to the excessive flow rate of the evaporated gas is supplied to the first oil separator 92, The driving reliability of the remelting device 90 can be improved and the driving efficiency can be increased due to the complete removal of the lubricating oil.

Also, unlike the embodiment of the present invention, the first oil separator 92 may be omitted and only the second oil separator 93 may be provided. In this case, since the second oil separator 93 does not need to remove the lubricating oil to the evaporative gas to be supplied to the power generation engine 50a and the gas combustion device 50b, which can be used even by using the evaporated gas mixed with the lubricating oil, The flow rate of the evaporation gas can be reduced and the size can be reduced, thereby reducing the construction cost and optimizing the system.

The control unit can control the standard high pressure evaporative gas compressor 40 (room temperature evaporative gas compressor) according to the amount of evaporative gas generated in the liquefied gas storage tank 10 and can control the standard high pressure evaporative gas compressor 40 according to the evaporative gas generation amount. Can be controlled to a standby state in which the compression of the evaporation gas is not realized.

Specifically, when the evaporation gas generation amount is equal to or less than the predetermined generation amount, the control unit controls either one of the standard high-pressure evaporative gas compressors 40 to be in a standby state and increases the remaining load of the standard high-pressure evaporative gas compressor 40 connected in parallel Can be controlled.

At this time, the predetermined generation amount is the amount of evaporated gas flowing into the standard high-pressure evaporative gas compressor 40 from the ineffective point of the standard high-pressure evaporative gas compressor 40, and the ineffective point of the standard high- Is a point at which the power consumption is not reduced even if the flow rate supplied to the standard high-pressure evaporative gas compressor (40) is decreased at the ratio of the flow rate of the flow rate of the refrigerant gas (40)

The load at the inefficiency point of the standard high-pressure evaporative gas compressor 40 may be 20 to 40% of the flow rate at which the standard high-pressure evaporative gas compressor 40 has the maximum load.

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: gas treatment system 100: ship
10: Liquefied gas storage tank 20: Boosting pump
21: forced vaporizer 22: high pressure pump
23: vaporizer 30: preheater
31: auxiliary preheater 40: standard high pressure evaporative gas compressor
41: first evaporative gas compressor 42: second evaporative gas compressor
43: third evaporative gas compressor 44: fourth evaporative gas compressor
45: Fifth evaporative gas compressor 40a: Cryogenic evaporative gas compressor
50: Propulsion engine 50a: Power generation engine
50b: Gas Combustion Apparatus (GCU) 51: Buffer tank
60: Oil storage tank 61: Oil pump
70: evaporation gas heat exchanger 81: first block valve
82: second block valve 83: third block valve
84: fourth block valve 90: re-liquefying device
91: Reducing valve 92: First oil separator
93: Second oil separator
L1: forced vaporization gas supply line L2: evaporation gas supply line
L2a: Power generation engine fuel supply line L3: Oil supply line
L4: Liquefied gas supply line L5: Re-liquefaction line
L5a: Power generation engine fuel supply line L5b: Gas combustion device fuel supply line
BL1: first bypass line BL2: second bypass line
BL3: Third bypass line B1: First control valve
B2: Second control valve P: Pressure sensor
F: Flow sensor L: Load sensor

Claims (9)

An evaporative gas compressor for supplying evaporative gas generated from a liquefied gas storage tank to a customer and provided in parallel and constructed in parallel with each other; And
And a buffer tank provided downstream of the evaporative gas compressor,
The evaporative gas compressor includes:
At least one of which is controlled to be in a stand-by state which does not implement an interruption state or a compression of the evaporation gas,
The buffer tank includes:
Wherein the evaporative gas compressors temporarily store the evaporative gases discharged at different pressures in the plurality of evaporative gas compressors so as to have predetermined pressures required by the customer, and then supply the evaporative gases to the customer. The method according to claim 1,
An evaporation gas supply line connecting the liquefied gas storage tank and the demander and having the evaporative gas compressor;
A bypass line bypassing upstream from the buffer tank on the evaporation gas supply line; And
Wherein at least one of the evaporative gas compressors is controlled to be in a standby state or in a standby state in which the evaporation gas is not compressed in accordance with an amount of evaporative gas generated in the liquefied gas storage tank, Further comprising a control unit for controlling the flow of the evaporative gas downstream of the evaporative gas compressor according to the control signal,
Wherein,
And controlling the evaporation gas discharged from the evaporation gas compressor to flow to the bypass line when the amount of evaporation gas generated in the liquefied gas storage tank is equal to or greater than a preset generation amount,
And controls the evaporated gas discharged from the evaporative gas compressor to flow to the buffer tank when the amount of evaporated gas generated in the liquefied gas storage tank is less than a predetermined amount. 3. The method according to claim 2,
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. 4. The method of claim 3, 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 compressor according to claim 1,
Wherein the compressor comprises a constituent compressor in which four or five stages of pistons are connected in series, wherein the constituent compressors are provided by four first to fourth evaporative gas compressors and are connected in parallel with each other. 6. The method of claim 5,
Further comprising first to fourth evaporation gas supply lines connecting the liquefied gas storage tank and the demander and having the first to fourth evaporative gas compressors,
Wherein upstream and downstream of the first to fourth evaporative gas compressors on the first to fourth supply lines are provided in common with an upstream common line and a downstream common line. 7. The apparatus of claim 6, wherein the buffer tank comprises:
Wherein said downstream common line is provided on said downstream common line. 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 8.

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