KR102287816B1 - Volatile organic compounds treatment system and ship having the same - Google Patents

Abstract

The present invention relates to a VOC treatment system and a ship, comprising: a VOC treating unit for compressing VOC generated in an oil storage tank provided on a ship and supplying the same to an engine mounted on the ship; and a gas fuel treating unit for mixing a liquefied gas of a gas fuel storage tank provided on the ship with the VOC supplied to the engine, wherein the VOC treating unit includes a gas-liquid separator that separates the VOC mixed with the liquefied gas into a gaseous phase and a liquid phase and supplies the separated gaseous VOC to the engine, and further includes a control unit that monitors the gaseous VOC supplied to the engine by the gas-liquid separator, and controls the flow rate of the liquefied gas delivered to the VOC by the gas fuel treating unit.

Description

Volatile organic compounds treatment system and ship having the same}

The present invention relates to a volatile organic compound treatment system (hereinafter referred to as a VOC treatment system) and a ship.

In general, a crude oil carrier is a ship that transports crude oil mined from a production site in a plurality of crude oil storage cargo tanks to a consumer by sea, and is referred to as a tanker, oil tanker, oil tanker, etc., and a cargo that stores crude oil Depending on the size of the tank, it is also called VLCC, ULCC, etc.

These crude oil carriers sail with a sufficient amount of crude oil loaded in 3 to 5 cargo tanks arranged side by side in the front and rear direction of the hull, at this time, the crude oil stored in the cargo tank is a liquid hydrocarbon naturally produced underground Or it is called a purified thing.

However, such crude oil generates a large amount of volatile organic compounds (hereinafter referred to as VOCs) in the process of being loaded on the crude oil carrier and/or in the state loaded in the cargo tank of the crude oil carrier.

The VOC generated in this way is very harmful to the human body, and when it is released into the atmosphere, it causes air pollution and environmental pollution by causing smog, etc. there is

Therefore, in recent years, various studies and developments have been continuously made on a method for recycling VOCs generated in a crude oil carrier without emitting it into the atmosphere, but an effective method has not yet been derived.

The present invention was created to solve the problems of the prior art as described above, and an object of the present invention is to solve the environmental pollution problem and prevent the waste of crude oil by using VOC generated from crude oil for propulsion of the hull, etc. To provide a processing system and a ship.

Another object of the present invention is to provide a VOC treatment system and a ship capable of increasing treatment efficiency by controlling control according to the amount of VOC generated from crude oil.

Another object of the present invention is to provide a VOC treatment system and a ship capable of suppressing unnecessary energy consumption by reabsorbing VOCs generated in the process of loading crude oil into a tank.

A VOC processing system according to an aspect of the present invention comprises: a VOC processing unit for compressing VOC generated in an oil storage tank provided on a ship and supplying it to an engine mounted on the ship; and a gas fuel processing unit for mixing the liquefied gas of the gas fuel storage tank provided in the ship with the VOC supplied to the engine, wherein the VOC processing unit separates the VOC in which the liquefied gas is mixed into a gas phase and a liquid phase. A control unit having a gas-liquid separator for supplying the VOC in the gas phase to the engine, monitoring the VOC in the gas phase supplied to the engine by the gas-liquid separator, and controlling the flow rate of the liquefied gas delivered to the VOC by the gas fuel processing unit; It is characterized in that it further comprises.

Specifically, the control unit may control the flow rate of the liquefied gas delivered to the VOC by the gas fuel processing unit by analyzing the load of the engine and the flow rate of VOC in the gas phase supplied to the engine by the gas-liquid separator. .

Specifically, the VOC processing unit may include: a VOC compressor for compressing the VOC discharged from the oil storage tank; and a mixer provided upstream or downstream of the VOC compressor to mix the liquefied gas with the VOC, wherein the control unit may control a flow rate of the liquefied gas delivered to the mixer by the gas fuel processing unit.

Specifically, the VOC processing unit further comprises a mixer provided downstream of the gas-liquid separator to mix liquefied gas with the VOC in the gas phase separated in the gas-liquid separator, wherein the control unit monitors the VOC upstream of the mixer to determine the It is possible to control the flow rate of the liquefied gas delivered to the VOC by the gas fuel processing unit.

According to another aspect of the present invention, there is provided a VOC processing system comprising: a VOC processing unit for compressing VOC generated in an oil storage tank provided on a ship and supplying it to an engine mounted on the ship; and a gas fuel processing unit for mixing the liquefied gas of the gas fuel storage tank provided in the ship with the VOC supplied to the engine, wherein the VOC processing unit has a VOC compressor for compressing the VOC discharged from the oil storage tank , a control unit that sets a dew point limit value of VOC for the VOC compressor, monitors the dew point of VOC sucked into the VOC compressor, and controls the flow rate of liquefied gas delivered to VOC by the gas fuel processing unit It is characterized in that it includes.

Specifically, the VOC processing unit further includes a mixer provided upstream of the VOC compressor to mix the liquefied gas with the VOC, and the control unit determines that the dew point of the VOC mixed with the liquefied gas in the mixer is below the dew point threshold. It is possible to control the flow rate of the liquefied gas delivered to the VOC by the gas fuel processing unit to maintain.

A ship according to an aspect of the present invention is characterized in that it has the VOC treatment system.

The VOC treatment system and the ship according to the present invention can effectively prevent environmental pollution by suppressing the VOC from being emitted to the atmosphere by using the VOC as a fuel for an engine.

In addition, the VOC processing system and the ship according to the present invention have the effect of maximizing the processing efficiency and energy consumption efficiency of VOC by changing the configuration of processing according to the generation time of VOC.

In addition, the VOC treatment system and the ship according to the present invention can reduce operating costs by recovering VOCs generated in the bunkering process into a tank so that there is no need to process the VOCs when loading is completed.

1 is a side view of a ship having a VOC treatment system according to first to fourth embodiments of the present invention;
2 is a conceptual diagram of a VOC processing system according to a first embodiment of the present invention.
3 is a conceptual diagram of a VOC processing system according to a second embodiment of the present invention.
4 is a conceptual diagram of a VOC processing system according to a third embodiment of the present invention.
5 is a conceptual diagram of a VOC processing system according to a fourth embodiment of the present invention.
6 is a side view of a ship having a VOC treatment system according to fifth and sixth embodiments of the present invention;
7 is a conceptual diagram of a VOC processing system according to a fifth embodiment of the present invention.
8 is a conceptual diagram of a VOC processing system according to a sixth embodiment of the present invention.
9 is a conceptual diagram of a ship including a VOC processing system according to seventh to eleventh embodiments of the present invention.
10 is a conceptual diagram of a VOC processing system according to a seventh embodiment of the present invention.
11 is a conceptual diagram of a VOC processing system according to an eighth embodiment of the present invention.
12 is a conceptual diagram of a VOC processing system according to a ninth embodiment of the present invention.
13 is a conceptual diagram of a VOC processing system according to a tenth embodiment of the present invention.
14 is a conceptual diagram of a VOC processing system according to an eleventh embodiment of the present invention.
15 is a conceptual diagram of a VOC processing system according to a twelfth embodiment of the present invention.
16 is a conceptual diagram of a VOC processing system according to a thirteenth embodiment of the present invention.
17 is a conceptual diagram of a VOC processing system according to a fourteenth embodiment of the present invention.
18 is a conceptual diagram of a VOC processing system according to a fifteenth embodiment of the present invention.
19 is a conceptual diagram of a VOC processing system according to a sixteenth embodiment of the present invention.
20 is a conceptual diagram of a VOC processing system according to a seventeenth embodiment of the present invention.
21 is a conceptual diagram of a ship including a VOC processing system according to an eighteenth embodiment of the present invention.
22 is a conceptual diagram of a ship including a VOC processing system according to a nineteenth embodiment of the present invention.
23 is a conceptual diagram of a ship including a VOC treatment system according to a nineteenth embodiment of the present invention.
24 is a conceptual diagram of a ship including a VOC processing system according to a nineteenth embodiment of the present invention.
25 is a conceptual diagram of a VOC processing system according to a nineteenth embodiment of the present invention.
26 is a conceptual diagram of a VOC processing system according to a twentieth embodiment of the present invention.
27 is a conceptual diagram of a VOC processing system according to the twenty-first and twenty-second embodiments of the present invention.
28 is a conceptual diagram of a VOC processing system according to a twenty-third embodiment of the present invention.
29 is a conceptual diagram of a VOC processing system according to a twenty-fourth embodiment of the present invention.

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

Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. Hereinafter, a VOC treatment system of the present invention will be described, and the present invention includes a VOC treatment system and a ship having the same.

At this time, it should be noted that ship is used in the meaning of encompassing all offshore plants such as FSRU and FPSO in addition to crude oil carriers that load crude oil that may generate VOC. In addition, the vessel may include a bunkering vessel for supplying crude oil to another vessel or land, etc. in addition to a vessel supplied to load or consume crude oil.

Hereinafter, liquefied gas is a substance that has a gaseous state at room temperature due to a lower boiling point than room temperature, and may be LPG, LNG, ethane, propane, butane, ethylene, ammonia, liquid nitrogen, and the like, and may mean, for example, LNG. In addition, hereinafter, oil or crude oil has a higher boiling point than room temperature, so it becomes liquid at room temperature and includes all substances used as fuel (crude oil, kerosene, heavy oil, light oil, etc.).

In addition, in the following, liquefied gas or boil-off gas is not limited to a liquid or gaseous phase despite the expression, and VOC is also not limited to a liquid or gaseous phase.

1 is a side view of a ship having a VOC processing system according to the present invention, and FIG. 2 is a conceptual diagram of a VOC processing system according to a first embodiment of the present invention.

1 and 2, the VOC processing system 1 according to the first embodiment of the present invention includes an oil storage tank (OT), a gas fuel storage tank (GT), and a VOC processing unit 10, These components may be mounted on the vessel (S).

The vessel S on which the VOC treatment system 1 is mounted includes a hull, and a cabin or an engine casing may be mounted on the stern side from the upper deck of the hull, and the engine (ME, GE, DE) on the stern side from the inside of the hull This can be provided.

At this time, the oil storage tank (OT) may be a cargo tank mounted on the inside of the ship (S), and thus the ship (S) may be a crude oil carrier. On the other hand, the gas fuel storage tank (GT) may be a high-pressure storage container mounted on the upper deck of the ship (S), and may be provided on each port and starboard.

In the present specification, the engine (ME, GE, DE) is an engine that consumes VOC, as a propulsion engine (ME) that propels the hull, is ME-GI, ME-GIE, ME-LGI, XDF, etc., and/or a ship ( S) may be a power generation engine (GE) that supplies power to the inside. However, it should be noted that the engine (ME, GE, DE) may be a concept encompassing all facilities (DE) that can consume VOC.

The oil storage tank OT is loaded with oil such as crude oil. Five or more oil storage tanks OT may be arranged in series in the longitudinal direction inside the hull, and the storage capacity of each oil storage tank OT is not particularly limited.

VOC generated from crude oil is present inside the oil storage tank OT, and the VOC may be, for example, a material containing components such as propane and butane.

In the conventional case, these explosive and toxic VOCs were simply discharged to the atmosphere or re-liquefied, stored and unloaded on land, but in this embodiment, in order to utilize the energy of VOCs, the engine (ME, GE, DE) can be operated.

To this end, the VOC discharge line 13 may be connected from the oil storage tank OT to the engines ME, GE, and DE, and the inlet end of the VOC discharge line 13 is opened at the upper inner side of the oil storage tank OT. may be placed in the

The gas fuel storage tank GT stores liquefied gas. As described above, when the ship (S) of the present invention is a crude oil carrier equipped with an oil storage tank (OT) as a cargo tank, the gas fuel storage tank (GT) may be mounted on the upper deck as a Type C type.

The liquefied gas stored in the gas fuel storage tank (GT) may be mixed with VOC generated in the oil storage tank (OT) and supplied to the engines (ME, GE, DE). A gas fuel supply line 23 may be provided up to the discharge line 13 , and a mixer 27 may be provided at a point where the gas fuel supply line 23 is connected to the VOC discharge line 13 . For reference, the components used to process gas fuel in this specification may be collectively referred to as the gas fuel processing unit 20 , and the gas fuel processing unit 20 and the VOC processing unit 10 hereinafter are the fuel processing units 10 and 20 . Note that it is covered by

The gas fuel storage tank GT may store liquefied gas at a high pressure, where the high pressure may mean a required pressure of the engines ME, GE, and DE. Therefore, since the liquefied gas discharged from the gas fuel storage tank GT may be in a state having the required pressure of the engines ME, GE, and DE, the VOC processing unit 10 to be described later is discharged from the gas fuel storage tank GT. Liquefied gas can be supplied to engines (ME, GE, DE) without separate compression (or through compression at a small ratio compared to VOC).

The VOC processing unit 10 supplies VOC generated from the oil storage tank OT as fuel of the engines ME, GE, and DE mounted on the ship S. To this end, the VOC processing unit 10 may include a VOC compressor 11 and a reformer 12 .

The VOC compressor 11 compresses the VOC. The VOC compressor 11 may compress the VOC to the required pressure of the engines ME, GE, and DE. can be determined in various ways. For example, the VOC compressor 11 may compress the VOC to about 10 to ME, GE, DE bar, or 100 to ME, GE, DE0 bar or the like.

The VOC compressor 11 may be provided in multiple stages, and an intercooler (not shown) may be provided between the VOC compressors 11 provided in multiple stages. In addition, the VOC compressors 11 may be provided in parallel to be able to back up each other.

The reformer 12 (reformer) reforms the compressed VOC and supplies it to the engines ME, GE, and DE. The reformer 12 may chemically treat VOCs including propane, butane, and the like, to methanate them.

Since the chemical action by the reformer 12 is already widely known, a detailed description thereof will be omitted. However, in this embodiment, the engines (ME, GE, DE) may be an engine that mainly consumes methane contained in LNG, and the reformer 12 uses various methods to convert VOCs into the fuel of the engines (ME, GE, DE). can be transformed into a suitable state.

The VOC processing unit 10 mixes the liquefied gas with the VOC and supplies it to the engines ME, GE, and DE, and in this case, the aforementioned mixer 27 may be used. The mixer 27 may be provided downstream of the reformer 12 on the VOC discharge line 13, and the VOC processing unit 10 mixes the VOC reformed by the reformer 12 with liquefied gas, thereby consuming methane. Even if a mixture of liquefied gas and VOC is supplied to the engine, it is possible to ensure that there is no problem in operation.

The VOC compressor 11 , the reformer 12 , and the mixer 27 may be provided on the VOC discharge line 13 , and the VOC discharge line 13 is from the oil storage tank OT to the engines ME and GE. , DE) to deliver the VOC. Of course, since VOC generated in the oil storage tank (OT) is reformed and then supplied to the engine (ME, GE, DE), the engine (ME, GE, DE) can be operated stably.

A gas fuel supply line 23 that delivers liquefied gas from the gas fuel storage tank GT to the engines ME, GE, and DE may be connected to the VOC discharge line 13 , and on the gas fuel supply line 23 , the gas A fuel vaporizer 22 may be provided.

The gas fuel vaporizer 22 may vaporize liquefied gas using various heat sources. The liquefied gas can be maintained in a liquid phase while being stored at a high pressure in the gas fuel storage tank (GT). ME, GE, DE) can be heated below the required temperature.

However, since the reformed VOC discharged by the reformer 12 may have a higher temperature (for example, 300 degrees to 500 degrees) than the required temperature of the engines ME, GE, and DE during the reforming process, the gas fuel vaporizer 22 ) can adjust the heating of the liquefied gas according to the temperature of the VOC discharged from the reformer 12 .

At this time, the control of the gas fuel vaporizer 22, in addition to the temperature of the VOC discharged from the reformer 12, the flow rate of VOC delivered to the engine (ME, GE, DE), the liquefied gas discharged from the gas fuel storage tank (GT) Of course, various sensors (not shown) may be provided in the VOC discharge line 13 and/or the gas fuel supply line 23 for this purpose.

The VOC compressor 11 compresses VOC to the required pressure of the engine (ME, GE, DE), and the gas fuel storage tank (GT) stores the liquefied gas at the required pressure of the engine (ME, GE, DE). The processing unit 10 mixes the liquefied gas discharged from the gas fuel storage tank GT with the VOC compressed by the VOC compressor 11 without separate compression (or through compression in a small ratio compared to the VOC compressor 11). can be supplied to the engines (ME, GE, DE).

As such, the present embodiment utilizes VOCs generated in the oil storage tank (OT) as fuel for engines (ME, GE, DE) operated by liquefied gas, and efficiently consumes VOCs to suppress environmental pollution, There is no need to prepare a facility for liquefying VOC, which can significantly reduce costs.

3 is a conceptual diagram of a VOC processing system according to a second embodiment of the present invention.

Referring to FIG. 3 , in the VOC processing system 1 according to the second embodiment of the present invention, a heat exchanger 16 may be provided instead of the mixer 27 when compared with the first embodiment.

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

The heat exchanger 16 may be provided in a two-stream structure having a flow path through which VOC flows, and a flow path through which liquefied gas flows. At this time, the flow path through which the VOC flows may be parallel to the VOC discharge line 13 , and the flow path through which the liquefied gas flows may be parallel with the gas fuel supply line 23 .

Since the VOC discharged from the reformer 12 may be in a very high temperature state, the present embodiment can reduce the temperature of the VOC to the required temperature of the engines ME, GE, and DE by using a relatively low temperature liquefied gas.

That is, the heat exchanger 16 cools the VOC while exchanging the VOC discharged from the reformer 12 with the liquefied gas, so that the reformed VOC is in a state suitable for the required temperature of the engines ME, GE, DE. .

However, on the contrary, since the temperature of the liquefied gas will rise due to heat exchange with VOC, the gas fuel vaporizer 22 can heat the liquefied gas to a temperature lower than the required temperature of the engine (ME, GE, DE) in consideration of this, Alternatively, the gas fuel vaporizer 22 itself may be omitted.

When the gas fuel vaporizer 22 is omitted, the heat exchanger 16 has a space in which liquefied gas is stored in a liquid phase, and high-temperature VOC flows inside the liquid liquefied gas while heating/vaporizing the liquefied gas and VOC is reduced. It may have a structure in the form of a water tank to be cooled. Of course, the structure of the heat exchanger 16 is not particularly limited.

In this embodiment, the VOC exhaust line 13 and the gas fuel supply line 23 may be provided in parallel to have a structure connected to the engines ME, GE, and DE, respectively. That is, the VOC is introduced into the engines ME, GE, and DE without being mixed with the liquefied gas, and may be mixed and used inside the engines ME, GE, and DE.

Of course, unlike the drawings, this embodiment is combined with the first embodiment so that the gas fuel supply line 23 is connected to the VOC exhaust line 13 downstream of the heat exchanger 16 and upstream of the engines ME, GE, DE. It may have a connected structure.

That is, in the present invention, the VOC, which has a higher temperature than the required temperature of the engine (ME, GE, DE) during the reforming process, is adjusted to the required temperature of the engine (ME, GE, DE) by using a relatively low temperature liquefied gas. All variants capable of cooling may be included.

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

Referring to FIG. 4 , the VOC treatment system 1 according to the third embodiment of the present invention further includes a VOC storage tank 15 .

The VOC storage tank 15 may temporarily store at least a portion of the compressed VOC. A VOC discharge line 13 is provided from the oil storage tank OT to the engines ME, GE, and DE, which is compressed by the VOC compressor 11 on the VOC discharge line 13 and then flows into the reformer 12. A portion of the previous VOC may be transferred to the VOC storage tank 15 along the VOC storage line 151 and stored in the VOC storage tank 15 .

At least a portion of the VOC flows into the VOC storage tank 15 without flowing into the reformer 12 from the downstream of the VOC compressor 11, so that the flow rate of VOC generated in the oil storage tank OT is This can be done if the amount that can be consumed in DE) is exceeded.

That is, according to the load of the engines (ME, GE, DE), a certain amount of VOC is delivered to the VOC storage tank 15 through the VOC storage line 151 branched from the upstream of the reformer 12 from the VOC discharge line 13 . can be

To this end, the VOC discharge line 13 may be provided with a flow meter 131 for measuring the flow rate of VOC, and a valve (not shown) is provided in the VOC discharge line 13 and/or the VOC storage line 151 . Provided, the opening degree of the valve can be adjusted according to the load of the flow meter 131 and the engine (ME, GE, DE).

BOC generated in the gas fuel storage tank GT may be introduced into the VOC storage tank 15 . To this end, the boil-off gas supply line 26 may be connected from the gas fuel storage tank GT to the VOC storage tank 15 .

The VOC storage tank 15 may store surplus VOC that cannot be consumed by the engines (ME, GE, DE) and the boil-off gas generated in the gas fuel storage tank (GT), and the VOC storage tank 15 is an oil VOC, etc. can be stored at a higher pressure than the storage tank (OT). In particular, the internal pressure of the VOC storage tank 15 may be adjusted according to the amount of BOG delivered.

A mixture of VOC and boil-off gas stored in the VOC storage tank 15 is transferred to the reformer 12 to be supplied to the engines ME, GE, and DE if necessary. From the VOC storage tank 15 to the reformer 12, a VOC supply line 152 may be provided, and the mixture is stored in the VOC storage tank 15, and the operating load of the engines (ME, GE, DE), oil According to conditions such as the flow rate of VOC discharged from the storage tank OT, the remaining amount of liquefied gas in the gas fuel storage tank GT, it may be transferred to the reformer 12 .

As the reformer 12, the VOC discharge line 13 and the VOC supply line 152 may be individually connected, and in contrast to the VOC transferred from the VOC discharge line 13 to the reformer 12, the VOC supply line 152 from the reformer. The mixture passed to (12) has a higher proportion of methane. In this case, the reformer 12 may be reformed in consideration of the VOC and the components of the mixture, respectively, and a known technique may be used for detailed chemical action.

In addition, the pressure of the mixture may be higher compared to the VOC introduced into the reformer 12. In this embodiment, the VOC discharge line 13 and the VOC supply line 152 connected to the reformer 12 have pressure gauges 132 and 233 respectively. ), the VOC compressor 11 and various valves (not shown) can be controlled in consideration of the pressure difference.

As such, in this embodiment, when surplus VOC is generated, it is stored in the VOC storage tank 15 together with the boil-off gas, and then supplied to the engines (ME, GE, DE) and used to increase system efficiency. there is.

5 is a conceptual diagram of a VOC processing system according to a fourth embodiment of the present invention.

Referring to FIG. 5 , the VOC treatment system 1 according to the fourth embodiment of the present invention includes a VOC storage tank 15 similar to the third embodiment, but unlike the previous embodiments, gas fuel storage The tank (GT) may not be included.

That is, in this embodiment, VOC generated in the oil storage tank (OT) is supplied to the engine (ME, GE, DE) through the VOC compressor 11 and the reformer 12, or at least a portion of the VOC is supplied to the VOC compressor ( 11) and then stored in the VOC storage tank 15, in which case the VOC storage tank 15 may be a tank for storing VOCs made of propane, butane, and the like.

The VOC stored in the VOC storage tank 15 may be supplied to the engines ME, GE, and DE through the reformer 12 if necessary. In this case, the VOC supply line 152 may be connected from the VOC storage tank 15 to the reformer 12 or the VOC discharge line 13 .

As a modified example, the VOC storage tank 15 is provided on the VOC discharge line 13 so that the VOC storage tank 15 serves as a buffer tank between the oil storage tank OT and the reformer 12, , the VOC storage line 151 or the VOC supply line 152 may not be provided.

Also as a modified example, when the engines ME, GE, and DE are engines that consume propane or butane rather than engines that consume methane, the reformer 12 may be omitted in this embodiment. However, in order to adjust the VOC to the required temperature of the engine (ME, GE, DE), etc., a heater (not shown) that heats the VOC using a non-limited heat medium such as seawater may be provided instead of the reformer 12 . there is.

As described above, in this embodiment, the VOC is removed from the oil storage tank (OT), stored, and then used, so that stable operation is possible regardless of the change in the amount of VOC emission.

6 is a side view of a ship having the VOC processing system according to the fifth and sixth embodiments of the present invention, and FIG. 7 is a conceptual diagram of the VOC processing system according to the fifth embodiment of the present invention.

Referring first to FIG. 6 , a ship S having a VOC treatment system 1 according to the present invention includes an oil storage tank OT, a VOC liquefier 14 , a VOC storage tank 15 , and a gas fuel storage tank. (GT).

The oil storage tank (OT) is provided in the ship in the ship (S) and may be arranged in plurality in the longitudinal direction of the hull. Oil such as crude oil stored in the oil storage tank OT may be in a liquid state, and may be stored at room temperature.

However, VOCs (propane, butane, etc.) having a boiling point higher than room temperature are mixed in crude oil stored in the oil storage tank (OT), and these VOCs are evaporated in the oil storage tank (OT). At this time, the evaporated VOC may be processed by the VOC liquefier 14 and delivered to the VOC storage tank 15 .

The VOC liquefier 14 liquefies the VOC generated from the oil storage tank OT and delivers it to the VOC storage tank 15 . When the VOC evaporates from the crude oil in the oil storage tank OT, the VOC may be discharged to the outside for durability of the oil storage tank OT, etc.

To this end, a VOC discharge line 13 is provided in the oil storage tank OT, and the VOC discharge line 13 is connected to the VOC liquefier 14 . The VOC liquefier 14 may receive and cool the VOC in a gaseous state, and the cooled VOC may be liquefied to significantly reduce the volume.

In order to liquefy the VOC, various types of refrigerants without limitation may be used. For example, the refrigerant may be nitrogen, liquefied gas, R134a, propane, or the like. The VOC liquefier 14 may be a type of heat exchanger that heats the refrigerant with VOC in a gaseous state.

The VOC storage tank 15 stores VOCs generated from the oil storage tank OT provided in the ship S. The VOC storage tank 15 can store VOC in a liquid state liquefied in the VOC liquefier 14 after being discharged in a gaseous state from the oil storage tank (OT), and is insulated to prevent re-evaporation of VOC. Or it may have the form of a high pressure vessel to increase the boiling point.

The VOC storage tank 15 may be provided onboard the ship (S), for example, it may be provided on the upper deck. Alternatively, the VOC storage tank 15 may be provided other than where the oil storage tank (OT) is disposed in the space inside the ship, for example, it may be provided in the engine room or between the engine room and the ship side shell plate.

VOC discharged from the oil storage tank OT and stored in the VOC storage tank 15 may be used as fuel for the engines ME, GE, and DE provided in the ship S. However, since VOC alone may have a low methane number and thus the efficiency may be reduced, the present invention is to increase the operating efficiency of the engine (ME, GE, DE) by ensuring the methane number, by mixing the liquefied gas with the VOC to increase the engine (ME). , GE, DE).

The gas fuel storage tank GT stores liquefied gas. When the ship (S) is a crude oil carrier equipped with an oil storage tank (OT) as a cargo tank, the gas fuel storage tank (GT) may be mounted on the upper deck in the form of Type C.

That is, the gas fuel storage tank (GT) may be a high-pressure storage container mounted on the upper deck, placed in front of the cabin on the upper deck, and may be provided on port and/or starboard.

The liquefied gas stored in the gas fuel storage tank (GT) may be mixed with the VOC of the VOC storage tank (15) and supplied to the engines (ME, GE, DE), and for this purpose, the engine ( An auxiliary tank 155 to be described later is provided between ME, GE, and DE, and a gas fuel supply line 23 may be provided between the auxiliary tank 155 in the gas fuel storage tank GT, and gas fuel is supplied. A one-way valve (not shown) and a flow meter 231 are provided on the line 23 .

The gas fuel storage tank GT can store liquefied gas at a high pressure. At this time, when the internal pressure of the gas fuel storage tank GT is greater than or equal to the required pressure of the engines ME, GE, DE, a gas fuel pump 21 to be described later. may be omitted.

Referring to FIG. 7 , the VOC processing system 1 according to the fifth embodiment of the present invention mixes the VOC and liquefied gas stored in the VOC storage tank 15 and the gas fuel storage tank GT, respectively, and the engine ME , GE, DE) includes a fuel processing unit (10, 20) for supplying the fuel.

For reference, the fuel processing units 10 and 20 include a VOC processing unit 10 covering components used to process VOC, and a gas fuel processing unit 20 covering components used for processing gas fuel. .

At this time, the engines (ME, GE, DE) are mounted on the ship (S) and may be a propulsion engine (ME) that propels the ship (S) or a power generation engine (GE, DE) that supplies power in the ship (S). In one example, the propulsion engine (ME) is an X-DF engine having a required pressure of 10 to 50 bar (for example, around 16 bar), and the power generation engine (GE, DE) has a required pressure of 1 to 10 bar (for example, around 6 bar). It may be a DFDE engine with

The fuel processing units 10 and 20 may adjust the methane number of the fuel supplied to the engines ME, GE, and DE by controlling the flow rates of VOC and liquefied gas. If the propulsion engine (ME) is an X-DF engine (Otto cycle engine), knocking may occur if VOC is used as the sole fuel because VOC has a low methane number.

Accordingly, the fuel processing units 10 and 20 may satisfy the methane number required for each load in the engines ME, GE, and DE by mixing the liquefied gas with the VOC in an appropriate ratio in order to prevent smooth combustion and knocking phenomenon.

To this end, the fuel processing units 10 and 20 may include a gas analyzer 232 , an auxiliary tank 155 , and a control unit 30 .

The gas analyzer 232 measures the methane number of the fuel supplied from the auxiliary tank 155 to the engines ME, GE, and DE. However, it should be noted that in the present specification, the methane number may be interpreted as encompassing all fuel specifications such as fuel components and calorific values in addition to the methane number. That is, the gas analyzer 232 of the present invention can be viewed as a calorimeter or a component measurer.

The auxiliary tank 155 mixes VOC and liquefied gas upstream of the engines ME, GE, and DE. A material in which VOC and liquefied gas are mixed in the auxiliary tank 155 may be referred to as a fuel in the present specification.

A gas fuel supply line 23 may be provided from the auxiliary tank 155 to the engines (ME, GE, DE), and the gas fuel supply line 23 requires the pressure of fuel from the engines (ME, GE, DE). A pressure gauge 233 may be provided to verify whether the pressure corresponds to the required pressure.

When the engine (ME, GE, DE) includes the X-DF propulsion engine (ME) and the DFDE power generation engine (GE, DE), the gas fuel supply line 23 is connected to the propulsion engine (ME) and the power generation engine (GE, DE). DE) may be branched downstream of the auxiliary tank 155 to be connected to. In this case, pressure regulating valves 234a and 234b (Pressure Regulating Valves) may be provided upstream of the propulsion engine ME and upstream of the power generation engines GE and DE in the downstream of the junction.

Since the fuel discharged from the auxiliary tank 155 may have a pressure matched to the higher required pressure among the required pressure of the propulsion engine ME and the required pressure of the power generation engines GE, DE, The pressure regulating valve 234b provided upstream may implement reduced pressure.

The auxiliary tank 155 can generate liquid fuel by mixing liquid VOC delivered through the VOC pump 154 and liquid liquefied gas delivered through the gas fuel pump 21 , and converts the fuel into a liquid phase to the engine. (ME, GE, DE) can be supplied. Alternatively, the auxiliary tank 155 may include a heater (not shown) for vaporizing the fuel in order to supply the fuel to the engines ME, GE, and DE in a gaseous phase.

The heater may be provided inside the auxiliary tank 155 or in a separate external line through which fuel circulates in the auxiliary tank 155 , and various substances such as steam or glycol water may be used. The fuel vaporized by the heater may be supplied to and consumed by the engines ME, GE, and DE through the pressure gauge 233 , the gas analyzer 232 , and the pressure control valves 234a and 234b .

The control unit 30 controls the flow rate of VOC and/or liquefied gas flowing into the auxiliary tank 155 . Therefore, the ratio of VOC and liquefied gas included in the fuel generated in the auxiliary tank 155 may be adjusted by the controller 30 .

The control unit 30 may control the flow rate of VOC and/or liquefied gas delivered to the auxiliary tank 155 in various ways. For example, a VOC pump 154 for delivering VOC to the engine (ME, GE, DE) is provided inside and/or outside the VOC storage tank 15, and the inside and/or outside of the gas fuel storage tank (GT) A gas fuel pump 21 for delivering liquefied gas to the engines ME, GE, and DE may be provided, and the controller 30 controls the VOC pump 154 and the gas fuel pump 21 .

At this time, the control unit 30 controls the VOC pump 154 and the gas fuel pump 21 according to the measured value of the gas analyzer 232 to calculate the methane number of the fuel generated in the auxiliary tank 155 to the engine (ME, GE, It can be adjusted to the level required by DE).

To this end, the VOC pump 154 and/or the gas fuel pump 21 may be provided to enable variable frequency control (VFD), but either the VOC pump 154 or the gas fuel pump 21 . It goes without saying that one is a fixed capacity type and the other is a variable capacity type. In this case, the controller 30 may control the variable displacement pump in consideration of the operation (On/Off) of the fixed displacement pump.

As described above, when the internal pressure of the gas fuel storage tank GT is greater than or equal to the required pressure of the engines ME, GE, DE, the gas fuel pump 21 may be omitted, so the control unit 30 controls the VOC pump 154 . Methane number can be adjusted through operation control. Of course, since a valve (not shown) may be provided on the gas fuel supply line 23 when the gas fuel pump 21 is omitted, the control unit 30 controls the VOC pump 154 and the gas fuel supply line 23 . Methane number control is possible through a valve on the top.

From the VOC storage tank 15 to the auxiliary tank 155, a VOC supply line 152 including a one-way valve (not shown) or a flow meter 156 may be provided, and in the VOC supply line 152 A VOC return line 157 for returning at least a portion of the VOC to the VOC storage tank 15 may be provided downstream of the VOC pump 154 . In this case, a VOC return valve 1571 that is a return valve may be provided on the VOC return line 157 .

In addition, a gas fuel return line 235 for returning at least a portion of the liquefied gas discharged from the gas fuel storage tank GT is provided in the gas fuel supply line 23 in the same/similar manner, and on the gas fuel return line 235 . A gas fuel return valve 236 that is a return valve may be provided.

In this case, the control unit 30 controls the VOC return valve 1571 and/or the gas fuel return valve 236 according to the measured value of the gas analyzer 232 , and by the VOC return valve 1571 , the engine ME, By adjusting the flow rate of VOC delivered to GE, DE) and/or the flow rate of liquefied gas delivered to the engine ME, GE, DE by the gas fuel return valve 236, the methane number of the fuel is adjusted to the engine (ME, GE, DE).

When the control unit 30 controls the VOC pump 154 and the gas fuel pump 21 and/or the VOC return valve 1571 and the gas fuel return valve 236 , the VOC and liquefaction flowing into the auxiliary tank 155 . Flowmeters 156 and 231 may be used to check whether the flow rate of gas is properly controlled, and flowmeters 156 and 231 may be provided in the VOC supply line 152 and the gas fuel supply line 23, respectively. .

Therefore, the control unit 30 measures the methane number of the fuel downstream of the auxiliary tank 155 to actively control the flow rate of VOC and liquefied gas flowing into the auxiliary tank 155, and verifies it through the flow meters 156 and 231. Adequate methane number can be guaranteed.

As described above, in this embodiment, the VOC, which was thrown into the atmosphere, is used as a fuel for the engine (ME, GE, DE), but the fuel specifications (methane number, calorific value, component, etc.) required by the engine (ME, GE, DE) are By mixing liquefied gas with VOC and supplying it to engines (ME, GE, DE) to satisfy the needs, VOCs can be reused while ensuring engine (ME, GE, DE) operating efficiency.

8 is a conceptual diagram of a VOC processing system according to a sixth embodiment of the present invention.

Referring to FIG. 8 , the VOC processing system 1 according to the sixth embodiment of the present invention mixes VOC with liquefied gas and supplies it to the propulsion engine ME, and only the liquefied gas is supplied to the power generation engines GE and DE. can supply Hereinafter, the present embodiment will be mainly described on the points that are different from the previous embodiment, and the parts omitted from the description will be replaced with the previous content.

In this embodiment, the propulsion engine (ME) may be a ME-GI engine having a required pressure of 200 to 400 bar (eg, around 380 bar). However, in the case of ME-GI engine, if only VOC (the amount of heat generated per volume injected into the engine (ME, GE, DE) is higher than that of methane, the main component of liquefied gas), the energy density becomes too high. can guarantee

In order to match the required pressure of the ME-GI engine, the VOC supply line 152 between the VOC storage tank 15 and the auxiliary tank 155 and the gas fuel between the gas fuel storage tank GT and the auxiliary tank 155 . On the supply line 23, a VOC high-pressure pump 158 and a gas fuel high-pressure pump 24 may be provided, respectively, and the high-pressure VOC and high-pressure liquefied gas are mixed to form a one-phase propulsion engine (ME) without phase separation. In order to supply to, a mixer 27 may be provided in place of the auxiliary tank 155 of the previous embodiment.

However, when the VOC pump 154 and the gas fuel pump 21 pressurize the VOC to a high pressure in accordance with the required pressure of the propulsion engine ME, or the auxiliary tank 155 rather than the mixer 27, the auxiliary tank ( When only one high-pressure pump (not shown) is provided downstream of 155 , the VOC high-pressure pump 158 and the gas-fuel high-pressure pump 24 may be omitted.

Between the VOC pump 154 and the mixer 27 and between the gas fuel pump 21 and the mixer 27 , a VOC vaporizer 159 and a gas fuel vaporizer 22 may be provided, respectively. The VOC vaporizer 159 and the gas fuel vaporizer 22 may respectively heat VOC and liquefied gas in response to the required temperature of the propulsion engine ME. Of course, it is also possible to provide a single heat exchanger (not shown) downstream of the mixer 27 instead of the VOC vaporizer 159 and the gas fuel vaporizer 22 .

In this embodiment, a gas fuel branch line 25 may be provided from the gas fuel supply line 23 to the power generation engines (GE, DE), and the gas fuel branch line 25 is a gas fuel pump 21 and gas fuel. It is branched from the gas fuel supply line 23 between the high-pressure pumps 24 to deliver the liquefied gas to the power generation engines GE and DE.

In the case of the previous embodiment, if the pressure difference between the required pressure of the propulsion engine (ME) and the power generation engine (GE, DE) was at a level that could be covered by the pressure control valve (234b), in the case of this embodiment, the required pressure of the propulsion engine (ME) was 200 bar Since the high pressure is higher than that, it may be difficult to resolve the pressure difference required between the propulsion engine ME and the power generation engines GE and DE through the pressure control valve 234b.

Therefore, in this embodiment, the line is branched, and a gas fuel high pressure pump 24 is provided on the propulsion engine ME side to match the required pressure of the propulsion engine ME, and the gas fuel high pressure pump 24 is pressurized to a high pressure. By supplying the liquefied gas to the power generation engine (GE, DE) side, it is possible to match the required pressure of the power generation engine (GE, DE).

Even in this configuration, pressure control valves 234a and 234b may be provided upstream of the propulsion engine ME and the power generation engines GE and DE, respectively, as well as a pressure control valve 234b in the gas fuel branch line 25 . ) in addition to the gas fuel heater 251 may be provided.

As such, in this embodiment, when using a high-pressure propulsion engine (ME) of 200 bar or more, by adjusting the energy density by mixing liquefied gas with the VOC, the operation efficiency of the propulsion engine (ME), etc. can be guaranteed while utilizing the VOC without discarding it. there is.

9 is a conceptual diagram of a ship including a VOC processing system according to seventh to eleventh embodiments of the present invention, FIG. 10 is a conceptual diagram of a VOC processing system according to a seventh embodiment of the present invention, and FIG. is a conceptual diagram of a VOC processing system according to an eighth embodiment.

12 is a conceptual diagram of a VOC processing system according to a ninth embodiment of the present invention, FIG. 13 is a conceptual diagram of a VOC processing system according to a tenth embodiment of the present invention, and FIG. 14 is an eleventh embodiment of the present invention It is a conceptual diagram of a VOC processing system according to the following.

Before describing in detail the VOC processing system 1 according to the embodiment of the present invention, a vessel S having the VOC processing system 1 according to the embodiment of the present invention will be described with reference to FIG. 9 first. let it do

Referring to FIG. 9 , a vessel S having a VOC treatment system 1 according to an embodiment of the present invention includes an oil storage tank OT, a VOC storage tank 15, a gas fuel storage tank GT, and a VOC It includes a processing unit 10 , demand destinations ME, GE, DE, and a seawater pump 40 .

The oil storage tank (OT) is provided in the ship in the ship (S) and may be arranged in plurality in the longitudinal direction of the hull. Oil such as crude oil stored in the oil storage tank OT may be in a liquid state, and may be stored at room temperature.

However, VOC (propane, butane) having a boiling point higher than room temperature is mixed in crude oil stored in the oil storage tank (OT), and these VOCs are evaporated in the oil storage tank (OT). At this time, the evaporated VOC may be processed by the VOC processing unit 10 and delivered to the VOC storage tank 15 .

The VOC storage tank 15 stores VOCs generated from the oil storage tank OT provided in the ship S. The VOC storage tank 15 may store VOC in a liquid state liquefied in the VOC processing unit 10 after it is discharged in a gaseous state from the oil storage tank OT, and is insulated to prevent re-evaporation of VOC or Or it may have the form of a high-pressure vessel to increase the boiling point.

The VOC storage tank 15 may be provided onboard the ship (S), for example, may be provided on the upper deck. Alternatively, the VOC storage tank 15 may be provided other than where the oil storage tank OT is disposed in the ship space, for example, may be provided in the engine room or between the engine room and the ship side outer plate.

VOC discharged from the oil storage tank OT and stored in the VOC storage tank 15 may be used as fuel for the main engine ME or the power generation engine GE provided in the ship S. However, since the VOC alone may have a low methane number and thus the efficiency may be reduced, the present invention provides a separate reformer (reformer 12 )), after adjusting the methane number, it can be supplied to the main engine (ME) or power generation engine (GE), or liquefied gas can be mixed with VOC and supplied to the main engine (ME) or power generation engine (GE).

The gas fuel storage tank GT stores liquefied gas. When the ship (S) is a crude oil carrier equipped with an oil storage tank (OT) as a cargo tank, the gas fuel storage tank (GT) may be mounted on the upper deck in the form of Type C.

That is, the gas fuel storage tank (GT) may be a high-pressure storage container mounted on the upper deck, placed in front of the cabin on the upper deck, may be provided on the port and/or starboard.

The liquefied gas stored in the gas fuel storage tank GT may be supplied to the VOC processing unit 10 and used to cool the VOC, and is also mixed with the VOC of the VOC storage tank 15 to the main engine ME or the power generation engine. (GE) can be supplied.

The VOC processing unit 10 liquefies the VOC generated from the oil storage tank OT and delivers it to the VOC storage tank 15 or to the consumers ME, GE, DE. When the VOC evaporates from the crude oil in the oil storage tank OT, the VOC may be discharged to the outside for durability of the oil storage tank OT, since the VOC may be a problem by increasing the pressure of the oil storage tank OT.

To this end, a VOC discharge line 13 is provided in the oil storage tank OT, and the VOC discharge line 13 is connected to the VOC processing unit 10 . The VOC processing unit 10 may receive VOC in a gaseous state to cool it, and the cooled VOC may be liquefied to significantly reduce its volume.

For the VOC processing unit 10, the configuration of each embodiment will be described in detail below with reference to FIGS. 10 to 14 .

Demanders (ME, GE, DE) may consume liquefied gas, boil-off gas, or VOC, and may include a main engine (ME), a power generation engine (GE), and other demanders (DE).

The main engine (ME) generates the power required to propel the ship (S) and can be, for example, a low-speed two-stroke low-pressure gas injection engine (X-DF) having a required pressure of 10 to 50 bar (for example, around 16 bar). there is.

The power generation engine GE generates electric power required for the ship S, and may be, for example, a heterogeneous fuel engine (DFDE) engine having a required pressure of 1 to 10 bar (eg, about 6 bar).

The other consumer (DE) consumes the gas component of VOC, and may be, for example, a boiler or a gas combustion unit. At this time, the gas component of VOC may be discharged to the atmosphere or may be stored in any storage medium in a compressed state. However, in the following, the other demanders (DE) may be replaced by the main engine (ME) or the power generation engine (GE).

The seawater pump 40 is disposed on the deck inside the stern of the ship (S) and can be connected through the VOC processing unit 10 seawater supply line (not shown), and through the seawater supply line Sea Chest It can be supplied to the VOC processing unit 10 by pumping seawater from the .

The seawater pump 40 may supply seawater to the VOC processing unit 10 so that the seawater can be used to cool the VOC, and as the VOC processing unit 10 is disposed on the upper deck, the height difference with the seawater pump 40 is A certain pressure can be applied to the seawater to compensate for the height head that may be caused by it.

10 is a conceptual diagram of a VOC processing system according to a seventh embodiment of the present invention.

Referring to FIG. 10 , the VOC processing system 1 according to the seventh embodiment of the present invention includes a first VOC compressor 11a , a second VOC compressor 11b , and a first heat exchanger corresponding to the VOC processing unit 10 . (16a), the second heat exchanger (16b), including a gas-liquid separator (17), and further includes a gas fuel processing unit (20) and a control unit (30).

Before describing the individual components of the VOC processing system 1 according to the seventh embodiment of the present invention, basic flow paths that organically connect the individual components will be described. Here, the flow path is a passage through which the fluid flows and may be a line.

The VOC treatment system 1 according to the seventh embodiment of the present invention may further include a first VOC discharge line 13a and a second VOC discharge line 13b.

Valves (not shown) capable of adjusting the opening degree may be installed in each line, and the supply amount of boil-off gas or liquefied gas may be controlled according to the control of the opening degree of each valve.

The first VOC discharge line 13a is connected to the VOC discharge line 13 connected from the oil storage tank OT to connect the gas-liquid separator 17, and to be formed in parallel with the second VOC discharge line 13b. and may include a first VOC compressor 11a and a first heat exchanger 16a.

The second VOC discharge line 13b is connected to the VOC discharge line 13 connected from the oil storage tank OT to connect the gas-liquid separator 17, and to be formed in parallel with the first VOC discharge line 13a. and may include a second VOC compressor 11b and a second heat exchanger 16b.

At this time, a three-way valve (not shown) may be disposed at a position where the first and second VOC discharge lines 13a and 13b are branched from the VOC discharge line 13, and the first VOC according to the adjustment of the opening degree of the three-way valve Whether VOC is supplied to the discharge line 13a or the second VOC discharge line 13b may be controlled.

Hereinafter, individual components that are organically formed by each of the above-described lines 13a and 13b to implement the VOC processing system 1 will be described.

The first VOC compressor 11a compresses VOC generated from the oil storage tank OT provided in the ship S, and may be disposed in parallel with the second VOC compressor 11b. Here, the first VOC compressor 11a may have a larger processing capacity than the second VOC compressor 11b, and may be operated at the time of loading crude oil to the oil storage tank OT.

Specifically, the first VOC compressor 11a is provided upstream of the first heat exchanger 16a on the first VOC discharge line 13a, receives the VOC generated from the oil storage tank OT and compresses it. It can be supplied to the first heat exchanger (16a).

The second VOC compressor 11b compresses VOC generated from the oil storage tank OT provided in the ship S, and may be disposed in parallel with the first VOC compressor 11a. Here, the second VOC compressor 11b may have a smaller processing capacity than the first VOC compressor 11a, and may be operated at the time of transporting the crude oil to the oil storage tank OT after loading it.

Specifically, the second VOC compressor 11b is provided upstream of the second heat exchanger 16b on the second VOC discharge line 13b, receives the VOC generated from the oil storage tank OT and compresses it. It can be supplied to the second heat exchanger (16b).

The first heat exchanger 16a cools the VOC compressed in the first VOC compressor 11a through the seawater supplied from the seawater pump 40 . Here, the first heat exchanger 16a may supply more cooling heat than the second heat exchanger 16b, and may be operated at the time of loading crude oil to the oil storage tank OT.

The first heat exchanger 16a exchanges heat with seawater compressed from the first VOC compressor 11a, supplies the heat-exchanged VOC to the gas-liquid separator 17, and the heat-exchanged seawater can be discharged to the sea. there is.

The second heat exchanger 16b cools the VOC compressed in the second VOC compressor 11b through the liquefied gas or boil-off gas supplied from the gas fuel storage tank GT. Here, the second heat exchanger 16b may supply less cooling heat than the first heat exchanger 16a, and may be operated at the time of transporting the crude oil to the oil storage tank OT after completing the shipment.

The second heat exchanger 16b exchanges heat between the VOC compressed from the second VOC compressor 11b and liquefied gas or boil-off gas, and supplies the heat-exchanged VOC to the gas-liquid separator 17, and the heat-exchanged liquefied gas or boil-off gas is It may be supplied to the gas fuel processing unit 20 to be used as fuel for the main engine ME or the power generation engine GE.

The gas-liquid separator 17 may receive VOC cooled and at least partially reliquefied from the first and second heat exchangers 16a and 16b, and may be separated into a gaseous phase and a liquid phase.

The gas-liquid separator 17 may supply the separated gaseous VOC to other consumers (DE), and the separated liquid VOC may be supplied to the VOC storage tank 15 .

The gas fuel processing unit 20 receives the VOC stored in the VOC storage tank 15 and the liquefied gas or boil-off gas heat-exchanged with the VOC from the VOC and the second heat exchanger 16b, the main engine (ME) or the power generation engine (GE) This can be treated as usable fuel.

To this end, the gas fuel processing unit 20 may include a gas fuel pump 21 for processing liquefied gas or boil-off gas, a gas fuel vaporizer 22, and the like.

The gas fuel pump 21 may receive the heat-exchanged liquefied gas from the second heat exchanger 16b and pressurize it according to the pressure required by the main engine ME or the power generation engine GE. At this time, when the gas heat-exchanged from the second heat exchanger 16b is boil-off gas, it can be compressed according to the pressure required by the main engine ME or the power generation engine GE by a separately provided boil-off gas compressor (not shown). can

The gas fuel vaporizer 22 may vaporize the liquefied gas supplied from the gas fuel pump 21 and may be heated to a temperature required by the main engine ME or the power generation engine GE.

The gas fuel processing unit 20 may further include a VOC compressor 11 and a reformer 12 that are a part of the VOC processing unit 10 .

The VOC compressor 11 may receive VOC from the VOC storage tank 15 and compress it to the required pressure of the main engine ME or the power generation engine GE, for example, may be compressed to about 10 to 50 bar.

The VOC compressors 11 may be provided in multiple stages, and an intermediate cooler may be provided between the VOC compressors 11 provided in multiple stages, and may be designed to be configured in parallel to back up each other.

The reformer 12 may reform the compressed VOC and supply it to the main engine ME or the power generation engine GE. The reformer 12 may be methanated by chemically treating VOCs including propane, butane, and the like. Since the chemical action by the reformer 12 is already widely known, a detailed description thereof will be omitted.

In addition, the gas fuel processing unit 20, a mixer 27 may be additionally installed. The mixer 27 is branched downstream of the reformer 12 and branched downstream of the vaporizer, and the VOC reformed by the reformer 12 is vaporized by the vaporizer or boil-off gas compressed by the boil-off gas compressor. After mixing with , it can be supplied to the main engine (ME) or the power generation engine (GE).

The control unit 30, the first and second VOC compressors 11a and 11b and the first and second heat exchangers 16a according to whether crude oil is loaded in the oil storage tank OT or whether crude oil is transported after shipment. , 16b) can be controlled to turn on or off.

At this time, the control unit 30 may be connected to the first and second VOC compressors 11a and 11b and the first and second heat exchangers 16a and 16b by wire or wirelessly to control them, and the VOC discharge line 13 . The first and second VOC discharge lines (13a, 13b) can be controlled by being connected to a three-way valve formed at a branching position by wire or wirelessly.

Specifically, the controller 30 controls the three-way valve when shipping crude oil to the oil storage tank OT to remove a large amount of VOC generated in the oil storage tank OT from the VOC discharge line 13 to the first VOC discharge line. After controlling to be supplied to (13a), after compressing a large amount of VOC through the first VOC compressor (11a), it can be controlled to be at least partially reliquefied by heat exchange with seawater through the first heat exchanger (16a) to cool it. .

In addition, the control unit 30 controls the three-way valve to discharge a small amount of VOC generated in the oil storage tank (OT) from the VOC discharge line (13) when the crude oil is shipped and then transferred to the oil storage tank (OT). After controlling to be supplied to the line 13b, a small amount of VOC is compressed through the second VOC compressor 11b and then cooled by heat exchange with liquefied gas or boil-off gas through the second heat exchanger 16b to be at least partially reliquefied. can be controlled At least some of the reliquefied VOC may be supplied to the gas-liquid separator 17 .

The driving according to the organic combination of each component of the VOC processing system 1 according to the seventh embodiment of the present invention described above will be described below with reference to FIGS. 10 (a) and (b).

10 (a) is a flow chart of VOC in the VOC processing system according to the seventh embodiment of the present invention when crude oil is shipped to the crude oil storage tank, and FIG. It is a flowchart of VOC in the VOC processing system according to the seventh embodiment of the present invention.

At the time of loading crude oil to the oil storage tank (OT), since a larger amount of VOC is generated than the amount of VOC generated in the process of transferring the crude oil to the oil storage tank (OT) after completing the shipment, a large amount of VOC Compressors and heat exchangers (cooling devices) that can treat

On the other hand, at the time of transporting after completing the shipment of crude oil to the oil storage tank (OT), a very small amount of VOC is generated than the amount of VOC generated in the process of shipping crude oil to the oil storage tank (OT). Compressors and heat exchangers (cooling devices) that can handle VOC of

However, it occurs at the time of loading crude oil into the oil storage tank (OT) because the transfer period after completing the shipment of crude oil to the oil storage tank (OT) is maintained longer than the time of loading the crude oil into the oil storage tank (OT). If only a compressor and a heat exchanger capable of processing the VOC are provided, energy is greatly wasted, the compressor is operated inefficiently, and there is a risk that the heat exchanger driving energy is wasted.

Accordingly, in the present invention, the loss of power consumed is prevented by dividing the VOC compressor 11 for compressing VOC and the heat exchanger for cooling VOC by processing capacity, and different types of compressors and heat exchangers driven according to the amount of VOC generated. It has the effect of consuming optimized energy.

That is, in the embodiment of the present invention, the first VOC compressor 11a and the first heat exchanger 16a using seawater having a large amount of cooling heat are driven at the time of loading crude oil to the oil storage tank (OT), It is consumed by driving the second VOC compressor 11b and the second heat exchanger 16b using liquefied gas or boil-off gas having a small amount of cooling heat at the time of transferring the crude oil to the oil storage tank (OT) after it is completed. It has the effect of preventing loss of power and consuming optimized energy.

Specifically, looking at the flow of the solid line in FIG. 10A , when crude oil is loaded into the oil storage tank OT, a large amount of VOC is generated in the oil storage tank OT. At this time, the oil storage tank OT supplies the VOC to the first VOC discharge line 13a through the VOC discharge line 13 .

The VOC supplied to the first VOC discharge line 13a is supplied to the first VOC compressor 11a and compressed, and then supplied to the first heat exchanger 16a to receive cooling heat from seawater and at least partially reliquefy it.

At least part of the reliquefied VOC is supplied to the gas-liquid separator 17 to be separated into gaseous and liquid phases, and the gaseous VOC is supplied to and consumed by other consumers (DE), and the liquid VOC is supplied to and stored in the VOC storage tank 15. .

Here, seawater heat-exchanged with VOC may be discharged back to the sea.

As described above, a large amount of VOC generated when crude oil is shipped to the oil storage tank (OT) can be mass-processed through the first VOC compressor 11a and the first heat exchanger 16a, so the stability of the system is improved. there is

Looking at the flow of the solid line in (b) of FIG. 10 , a small amount of VOC is generated in the oil storage tank OT when crude oil is shipped and then transferred to the oil storage tank OT. At this time, the oil storage tank OT supplies the VOC to the second VOC discharge line 13b through the VOC discharge line 13 .

The VOC supplied to the second VOC discharge line 13b is supplied to the second VOC compressor 11b and compressed, and then supplied to the second heat exchanger 16b to receive cooling heat from seawater and at least partially reliquefy it.

At least part of the reliquefied VOC is supplied to the gas-liquid separator 17 to be separated into gaseous and liquid phases, and the gaseous VOC is supplied to and consumed by other consumers (DE), and the liquid VOC is supplied to and stored in the VOC storage tank 15. .

As such, a small amount of VOC generated when crude oil is transported after shipping to the oil storage tank (OT) is not the first VOC compressor 11a and the first heat exchanger 16a, which have a large processing capacity, but a small amount of processing capacity. Eggplant can be processed through the second VOC compressor 11b and the second heat exchanger 16b, thereby optimizing the power consumption of the system and reducing energy waste.

Here, the liquefied gas or boil-off gas heat-exchanged with VOC is supplied to the gas fuel processing unit 20 and processed, and then used as fuel for the main engine (ME) or power generation engine (GE) or VOC supplied from the VOC storage tank 15 and It can be mixed and used as fuel for the main engine (ME) or the power generation engine (GE).

11 is a conceptual diagram of a VOC processing system according to an eighth embodiment of the present invention.

Referring to FIG. 11 , the VOC processing system 1 according to the eighth embodiment of the present invention is provided with a gas fuel liquefier 28 instead of the gas fuel processing unit 20 when compared to the seventh embodiment above. can

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

The gas fuel liquefier 28 may re-liquefy liquefied gas or boil-off gas through a refrigerant such as nitrogen, liquefied gas, R134a, or propane. Here, the liquefied gas refers to a liquefied gas that has been heated and vaporized.

The gas fuel liquefier 28 receives the boil-off gas or vaporized liquefied gas heated by heat exchange with the VOC compressed through the second heat exchanger 16b, and through a refrigerant such as nitrogen, liquefied gas, R134a, propane, etc. can be reliquefied.

The configuration and operation of the reliquefaction of the gas fuel liquefier 28 is already widely known, and detailed description thereof will be omitted.

11 (a) and (b) for the drive according to the organic combination of each component of the VOC treatment system 1 according to the eighth embodiment of the present invention through the above-described gas fuel liquefier 28 to be described below.

11 (a) is a flow chart of VOC in the VOC processing system according to the eighth embodiment of the present invention when crude oil is shipped to a crude oil storage tank, and (b) of FIG. It is a flowchart of VOC in the VOC processing system according to the eighth embodiment of the present invention.

In the eighth embodiment of the present invention, each VOC flow in FIGS. 11 (a) and (b), that is, when the crude oil is loaded into the oil storage tank (OT) or the crude oil is transferred to the oil storage tank (OT) after the shipment is completed. Since the flow of VOC of the city is all the same as that of the seventh embodiment, it will be replaced.

However, there is a difference in that the flow of boil-off gas or vaporized liquefied gas heated by heat exchange with VOC compressed through the second heat exchanger 16b is supplied to and consumed by the gas fuel liquefier 28 .

Due to this difference, in the embodiment of the present invention, the liquefied gas or boil-off gas heat-exchanged through the second heat exchanger 16b can be re-liquefied through the gas fuel liquefier 28, thereby reducing the waste of boil-off gas or liquefied gas. This has the effect of optimizing system utilization efficiency.

12 is a conceptual diagram of a VOC processing system according to a ninth embodiment of the present invention.

Referring to FIG. 12 , in the VOC processing system 1 according to the ninth embodiment of the present invention, the arrangement of the first and second VOC discharge lines 13a and 13b is different from that of the seventh embodiment, and the 2 Since the flow of VOC is changed differently according to the different driving times of the heat exchanger 16b, it will be mainly described.

The third VOC discharge line 13c, which is newly named here, is a line included in the first and second VOC discharge lines 13a and 13b in the previous embodiment, but in the previous embodiment and the first and second VOC discharge lines Note that it is only a new name to easily explain the difference between (13a, 13b).

The first VOC discharge line 13a includes a first VOC compressor 11a and a first heat exchanger 16a, and may be connected to the second heat exchanger 16b.

The first VOC discharge line 13a may be connected to the VOC discharge line 13 connected from the oil storage tank OT, and when crude oil is shipped to the oil storage tank OT, VOC through the VOC discharge line 13 can be supplied and a large amount of VOC can flow.

The second VOC discharge line 13b includes a second VOC compressor 11b and is connected to the second heat exchanger 16b.

The second VOC discharge line 13b may be connected to the VOC discharge line 13 connected from the oil storage tank OT, and the VOC discharge line 13 when transporting crude oil to the oil storage tank OT after completion of shipment. A small amount of VOC can flow by receiving VOC through the

The third VOC discharge line 13c connects the second heat exchanger 16b and the gas-liquid separator 17 and supplies at least partially reliquefied VOC to the gas-liquid separator 17 by heat exchange in the second heat exchanger 16b. can

In addition, in the embodiment of the present invention, the second heat exchanger 16b may be operated both when the crude oil is loaded into the oil storage tank OT or when the crude oil is transferred to the oil storage tank OT after the shipment is completed.

As described above, in the ninth embodiment of the present invention, since the second heat exchanger 16b can be additionally used to cool a large amount of VOC when crude oil is shipped to the oil storage tank OT, sufficient supply of the cooling medium becomes possible. There is an advantage in that the reliability of the liquefaction is improved and the first heat exchanger 16a can be backed up.

Of course, it is difficult to completely back up the first heat exchanger 16a due to the limitation of the processing capacity, but the backup is sufficiently possible during the maintenance or repair period of the first heat exchanger 16a.

12 ( It will be described below through a) and (b).

Figure 12 (a) is a flow chart of VOC in the VOC processing system according to the ninth embodiment of the present invention when crude oil is shipped to the crude oil storage tank, and Figure 12 (b) is, after shipping crude oil to the crude oil storage tank It is a flowchart of VOC in the VOC processing system according to the ninth embodiment of the present invention.

Looking at the flow of the solid line in (a) of FIG. 12 , when crude oil is loaded into the oil storage tank OT, a large amount of VOC is generated in the oil storage tank OT. At this time, the oil storage tank OT supplies the VOC to the first VOC discharge line 13a through the VOC discharge line 13 .

The VOC supplied to the first VOC discharge line 13a is supplied to the first VOC compressor 11a and compressed, and then supplied to the first heat exchanger 16a to receive cooling heat from seawater and at least partially reliquefy it.

At least some of the reliquefied VOC may be additionally supplied to the second heat exchanger 16b to be further cooled, through which complete reliquefaction may be achieved.

The VOC reliquefied in the second heat exchanger 16b is supplied to the gas-liquid separator 17 through the third VOC discharge line 13c to be separated into gas phase and liquid phase, and the VOC in the gas phase is supplied to and consumed by other consumers (DE). and liquid VOC is supplied to and stored in the VOC storage tank 15 .

Here, seawater heat-exchanged with VOC may be discharged back to the sea.

As described above, a large amount of VOC generated when crude oil is shipped to the oil storage tank (OT) can be mass-processed through the first VOC compressor 11a and the first heat exchanger 16a, so the stability of the system is improved. There is an effect of maximizing the re-liquefaction performance of VOC and improving the re-liquefaction reliability because it can be further cooled through the second heat exchanger 16b.

Looking at the flow of the solid line in (b) of FIG. 12 , a small amount of VOC is generated in the oil storage tank OT when crude oil is shipped and then transferred to the oil storage tank OT. At this time, the oil storage tank OT supplies the VOC to the second VOC discharge line 13b through the VOC discharge line 13 .

The VOC supplied to the second VOC discharge line 13b is supplied to the second VOC compressor 11b and compressed, and then supplied to the second heat exchanger 16b to receive cooling heat from seawater and at least partially reliquefy it.

At least part of the reliquefied VOC is supplied to the gas-liquid separator 17 through the third VOC discharge line 13c to be separated into gaseous and liquid phases. It is supplied to the storage tank 15 and stored.

As described above, a small amount of VOC generated when crude oil is transported after shipping to the oil storage tank (OT) can be processed through the second VOC compressor 11b and the second heat exchanger 16b having a small amount of processing capacity, It has the effect of optimizing the power consumption of the system and reducing energy waste.

Here, the liquefied gas or boil-off gas heat-exchanged with VOC is supplied to the gas fuel processing unit 20 and processed, and then used as fuel for the main engine (ME) or power generation engine (GE) or VOC supplied from the VOC storage tank 15 and It can be mixed and used as fuel for the main engine (ME) or the power generation engine (GE).

13 is a conceptual diagram of a VOC processing system according to a tenth embodiment of the present invention.

Referring to FIG. 13 , the VOC processing system 1 according to the tenth embodiment of the present invention is to be provided with a gas fuel liquefier 28 instead of the gas fuel processing unit 20 when compared to the ninth embodiment above. can

However, since this difference is the same as the difference from the seventh embodiment in the previous eighth embodiment, the configuration of the present embodiment and its effects can be fully understood through the eighth embodiment, so the description of the present embodiment will be omitted. .

14 is a conceptual diagram of a VOC processing system according to an eleventh embodiment of the present invention.

Referring to FIG. 14 , in the VOC processing system 1 according to the eleventh embodiment of the present invention, a gas-liquid separator (the first gas-liquid separator 17a) is additionally constructed in comparison with the ninth and tenth embodiments. Since they are different, we will focus on them.

The first VOC discharge line 13a includes a first VOC compressor 11a, a first heat exchanger 16a, and a first gas-liquid separator 17a, and may be connected to the second heat exchanger 16b.

The first VOC discharge line 13a may be connected to the VOC discharge line 13 connected from the oil storage tank OT, and when crude oil is shipped to the oil storage tank OT, VOC through the VOC discharge line 13 can be supplied and a large amount of VOC can flow.

The first gas-liquid separator 17a is built on the first VOC discharge line 13a to temporarily store at least partially reliquefied VOC, and can also separate at least partially reliquefied VOC into gas phase and liquid phase, VOC in the gas phase may be supplied to the second heat exchanger 16b again, and VOC in the liquid phase may be supplied to the VOC storage tank 15 .

The first gas-liquid separator 17a is used for shipping crude oil to the oil storage tank OT, and can temporarily store a large amount of VOC as described above, thereby serving as a flow buffer.

Since the second gas-liquid separator 17b is the same as the gas-liquid separator 17 described in the previous embodiment, a detailed description thereof will be omitted.

As such, in the eleventh embodiment of the present invention, the first gas-liquid separator 17a is additionally constructed to re-liquefy a large amount of VOC when crude oil is shipped to the oil storage tank (OT), so the flow rate required to process a large amount of VOC Since it can serve as a buffer, there is an advantage in that the reliability of VOC processing is improved.

Through the above-described configuration, the driving according to the organic combination of each configuration of the VOC processing system 1 according to the eleventh embodiment of the present invention will be described below with reference to FIGS. 6 (a) and (b).

Figure 14 (a) is a flow chart of VOC in the VOC processing system according to the eleventh embodiment of the present invention when crude oil is shipped to the crude oil storage tank, and Figure 14 (b) is, after shipping crude oil to the crude oil storage tank. It is a flowchart of VOC in the VOC processing system according to the eleventh embodiment of the present invention.

Looking at the flow of the solid line in (a) of FIG. 14 , when crude oil is loaded into the oil storage tank OT, a large amount of VOC is generated in the oil storage tank OT. At this time, the oil storage tank OT supplies the VOC to the first VOC discharge line 13a through the VOC discharge line 13 .

The VOC supplied to the first VOC discharge line 13a is supplied to the first VOC compressor 11a and compressed, and then supplied to the first heat exchanger 16a to receive cooling heat from seawater and at least partially reliquefy it.

At least some of the reliquefied VOC may be supplied to the first gas-liquid separator 17a and temporarily stored, and at this time, may be separated into a gaseous phase and a liquid phase.

The liquid phase separated in the first gas-liquid separator 17a may be supplied to the VOC storage tank 15 and the separated gas phase may be supplied to the second heat exchanger 16b to be further cooled and re-liquefied.

The VOC reliquefied in the second heat exchanger 16b is supplied to the second gas-liquid separator 17b through the third VOC discharge line 13c to be separated again into gaseous and liquid phases, and the gaseous VOCs are sent to other consumers (DE). It is supplied and consumed, and the liquid VOC is supplied to and stored in the VOC storage tank 15 .

Here, seawater heat-exchanged with VOC may be discharged back to the sea, and liquefied gas or boil-off gas heat-exchanged with VOC is supplied to the gas fuel processing unit 20 to fuel the main engine (ME) or power generation engine (GE). can be used as

As such, a large amount of VOC generated when crude oil is shipped to the oil storage tank (OT) can be mass-processed through the first VOC compressor 11a and the first heat exchanger 16a, and at the same time, the first gas-liquid separator ( 17a) can temporarily store a certain flow rate, which has the effect of preventing overload of each driving device, and also has the effect of improving the stability of the system, and can be further cooled through the second heat exchanger 16b This has the effect of maximizing the reliquefaction performance of VOC and improving the reliquefaction reliability.

Looking at the flow of the solid line in (b) of FIG. 14 , a small amount of VOC is generated in the oil storage tank OT when crude oil is shipped and then transferred to the oil storage tank OT. At this time, the oil storage tank OT supplies the VOC to the second VOC discharge line 13b through the VOC discharge line 13 .

The VOC supplied to the second VOC discharge line 13b is supplied to the second VOC compressor 11b and compressed, and then supplied to the second heat exchanger 16b to receive cooling heat from seawater and at least partially reliquefy it.

At least part of the reliquefied VOC is supplied to the second gas-liquid separator 17b through the third VOC discharge line 13c to be separated into gaseous and liquid phases, and the gaseous VOCs are supplied to and consumed by other consumers (DE), and VOCs in the liquid phase is supplied to and stored in the VOC storage tank 15 .

As described above, a small amount of VOC generated when crude oil is transported after shipping to the oil storage tank (OT) can be processed only through the second VOC compressor 11b and the second heat exchanger 16b having a small amount of processing capacity, It has the effect of optimizing the power consumption of the system and reducing energy waste.

Here, the liquefied gas or boil-off gas heat-exchanged with VOC is supplied to the gas fuel processing unit 20 and processed, and then used as fuel for the main engine (ME) or power generation engine (GE) or VOC supplied from the VOC storage tank 15 and It can be mixed and used as fuel for the main engine (ME) or the power generation engine (GE).

As described above, the VOC treatment system 1 and the ship S according to the present invention have the effect of maximizing the processing efficiency and energy consumption efficiency of VOC by changing the configuration of processing according to the generation time of VOC. .

15 is a conceptual diagram of a VOC processing system according to a twelfth embodiment of the present invention.

Referring to FIG. 15 , the VOC processing system 1 according to the twelfth embodiment of the present invention includes an oil storage tank OT, a gas fuel storage tank GT, a VOC processing unit 10 , and a gas fuel processing unit 20 . includes Hereinafter, the present embodiment will be mainly described in terms of differences from the previous content.

The VOC processing unit 10 processes the VOC generated in the oil storage tank OT storing oil such as crude oil and supplies it to the main engine ME or the power generation engine GE. To this end, the VOC processing unit 10 includes a VOC compressor 11 , a gas-liquid separator 17 , and the like.

The VOC compressor 11 compresses the VOC. The VOC compressor 11 can compress the VOC appropriately to the pressure required by the engine (ME, GE, DE), etc., and the VOC output from the VOC compressor 11 according to the type of the engine (ME, GE, DE). The pressure may be 10 bar to 600 bar or the like.

The VOC compressor 11 may be a variable compressor, and the compression ratio may be varied according to the loads of the engines ME, GE, and DE. That is, since the loads of the engines ME, GE, and DE may be determined differently depending on the ship speed to be paid by the ship S, the VOC compressor 11 may adjust the pressure of the VOC in consideration of the required ship speed.

Or, for example, when the main engine (ME) is XDF, the required pressure is around 18 bar, the required pressure of the power generation engine (GE) is 10 bar, and the required pressure of a boiler that is other demand (DE) may be 8 bar, so the VOC compressor ( 11) can adjust the compression of VOC in response to the required pressure of the engine (ME, GE, DE), etc.

Unlike the drawing, the mixer 27 is provided upstream of the main engine ME and upstream of the power generation engine GE, respectively, so that the main engine ME, the power generation engine GE, etc. In the case of a system in which VOC mixing is turned on/off for each engine (ME, GE, DE), whether the engine (ME, GE, DE) to which VOC is delivered is the main engine (ME) or the power generation engine (GE) Accordingly, the compression ratio of the VOC compressor 11 may vary.

Unlike the above, the VOC compressor 11 may be a fixed compressor, and the VOC compressor 11 may compress the VOC to a pressure (eg 7 to 10 bar) lower than the required pressure (eg 18 bar) of the main engine ME. there is.

Referring to the actual operation case, since the main engine (ME) was not operated at the maximum load, the fuel was compressed and consumed to a pressure less than the maximum required pressure. .

Therefore, the present invention compresses and supplies the VOC according to the required pressure of the power generation engine (GE), etc., which has a lower required pressure than the main engine (ME), based on the data of the actual operation case, and supplies power. You can save money without affecting the operation.

The gas-liquid separator 17 separates VOCs from gas-liquid. VOC is generally volatilized in the oil storage tank (OT) and discharged in a gaseous state, but as the VOC is compressed in the VOC compressor 11, a phase change may occur due to a pressure increase, and thus a liquid state may be mixed. Therefore, the gas-liquid separator 17 filters the liquid phase contained in the VOC and supplies only the gas phase to the engines ME, GE, DE, etc., thereby ensuring the engine (ME, GE, DE) efficiency.

For reference, liquid may be mixed into VOC upstream of the VOC compressor 11, but in this case, a knock-out drum is disposed at the front end of the VOC compressor to separate the liquid, and the vapor phase to the VOC compressor 11 can only be brought in.

However, when the oil is loaded into the oil storage tank (OT), the ship (S) does not propel, so there is no operation of the main engine (ME) for propulsion. Therefore, the VOC in the gas phase separated by the gas-liquid separator 17 may be returned to the oil storage tank OT, etc., like the VOC in the liquid phase, which will be described later.

A VOC discharge line 13 is connected from the oil storage tank (OT) to the gas-liquid separator 17, and the VOC discharge line 13 allows and controls the flow of VOCs based on the internal pressure of the oil storage tank (OT). can

A VOC recovery line 171 may be provided in the gas-liquid separator 17 , and the VOC recovery line 171 may recover the liquid VOC separated in the gas-liquid separator 17 to the oil storage tank OT. The VOC compressor 11 may compress VOC to 10 bar, for example. In this case, the liquid VOC (LVOC) in the gas-liquid separator 17 may be generated to about 6%.

The VOC recovery line 171 may be injected into the upper and/or lower portions of the oil storage tank OT, and the VOC compressed by the VOC compressor 11 flows into the internal space of the oil storage tank OT. The pressure is lowered and can be cooled by the Joule-Thomson effect.

Therefore, it is possible to slightly lower the internal temperature of the oil storage tank (OT) due to the return of the LVOC, thereby suppressing the occurrence of VOC. However, it is necessary to prevent the viscosity of the oil storage tank (OT) from increasing. Considering the amount (up to 98%) and the like, separate heating is not required despite the return of LVOC.

A CO2 adsorber 133 may be provided upstream of the VOC compressor 11 in the VOC discharge line 13 . The CO2 adsorber 133 removes CO2 from VOC and delivers it to a mixer 27 to be described later. That is, the VOC compressor 11 may compress the VOC from which CO2 has been removed by the CO2 adsorber 133 .

VOC is a component volatilized from oil such as crude oil, and as described above, heavy carbon (heavy hydrocarbons) such as propane and butane is the main component. However, the present invention intends to supply VOC to engines (ME, GE, DE) together with gas fuel such as LNG. Since the efficiency of engines (ME, GE, DE) driven by gas fuel is controlled by the methane number, the methane number When a large amount of low VOC flows, there is a risk that the operating efficiency of the engine (ME, GE, DE) may decrease.

In addition, VOC is heat exchanged and/or mixed with gas fuel and supplied to engines (ME, GE, DE). In this case, low-temperature corrosion may occur due to CO2 contained in VOC.

Therefore, in the present invention, by adsorbing and removing CO2 from VOC before compression, it is possible to slightly increase the methane number of VOC mixed with gas fuel, and also solve the low-temperature corrosion problem in the heat exchanger 16 or the mixer 27. there is.

Since the CO2 adsorber 133 can remove CO2 from VOCs using various methods currently known, the specific configuration of the CO2 adsorber 133 is not particularly limited. Also, of course, the CO2 adsorber 133 may be configured to remove CO2 by a method other than adsorption despite the terminology.

The gas fuel processing unit 20 supplies gas fuel such as LNG to the engines ME, GE, and DE. In the present invention, VOC may be mixed in addition to gas fuel and supplied to the engines ME, GE, and DE, and for this, the gas fuel processing unit 20 includes a mixer 27 .

The mixer 27 may mix VOC with gas fuel and supply it to the engines ME, GE, DE, etc. mounted on the ship S. At this time, the VOC delivered to the mixer 27 may be a vapor phase VOC (SVOC) separated by the gas-liquid separator 17 described above.

VOC in the gas phase introduced into the mixer 27 is compressed by the VOC compressor 11 and then gas-liquid separated. may be supplied to the engine (ME, GE, DE) after being adjusted.

To this end, the gas fuel processing unit 20 may include a gas fuel pump 21 or a gas fuel vaporizer 22 , and the above components may be appropriately disposed upstream and/or downstream of the mixer 27 .

The gas fuel processing unit 20 may include a gas fuel supply line 23 connected from the gas fuel storage tank GT to the mixer 27, and in the present invention, the engines ME, GE, and DE are basically gas Considering that it is a fuel-powered type, the line from the mixer 27 to the engines ME, GE, and DE may be referred to as a gas fuel supply line 23 .

The line connected from the gas fuel storage tank GT to the mixer 27 is together with the gas fuel supply line 23 through which liquid gas fuel flows, or instead of the gas fuel supply line 23, gas fuel is It may include a boil-off gas supply line 26 through which boil-off gas flows.

In this case, considering that the methane number is different for liquid gas fuel and gas fuel gas, depending on the load of the engine (ME, GE, DE), in addition to the VOC mixing ratio, the liquid and gaseous mixture ratio among gas fuels will also be adjusted. can Therefore, the methane number of the fuel flowing into the engines (ME, GE, DE) can be properly maintained.

As such, in this embodiment, after VOC is compressed, SVOC is mixed with gas fuel and supplied to engines (ME, GE, DE), etc., and LVOC is returned to the oil storage tank (OT), thereby suppressing the emission of VOC to the atmosphere. and reduce the consumption of gas fuel.

16 is a conceptual diagram of a VOC processing system according to a thirteenth embodiment of the present invention.

Referring to FIG. 16 , in the VOC processing system 1 according to the thirteenth embodiment of the present invention, the configuration of the VOC processing unit 10 may be different from that of the previous twelfth embodiment.

In the present embodiment, the VOC processing unit 10 further includes a heat exchanger 16 and a VOC storage tank 15 . The heat exchanger 16 cools the VOC generated in the oil storage tank OT. At this time, the refrigerant used by the heat exchanger 16 to cool the VOC is gas fuel, heat (glycol water, seawater, fresh water, etc.) used for vaporization of gas fuel, and/or fresh water for cooling used in the ship (S). etc., but is not particularly limited. However, in the present embodiment, for convenience, the heat exchanger 16 will be described by limiting the cooling of the VOC with gas fuel.

The heat exchanger 16 heats the VOC generated in the oil storage tank OT with gas fuel to cool it. To this end, the gas fuel supply line 23 may be branched from the gas fuel storage tank GT and connected to the heat exchanger 16 and the mixer 27, respectively.

Alternatively, unlike the drawing, the liquid gas fuel discharged from the gas fuel storage tank GT is delivered to the mixer 27 through the gas fuel supply line 23, mixed with the VOC, and then supplied to the engines ME, GE, DE. The gas fuel vaporized in the gas fuel storage tank (GT) is transferred to the heat exchanger 16 through the boil-off gas supply line 26, and after heat exchange with VOC, a gas combustion device (GCU, not shown), etc. can be burned by

That is, the gas fuel supply line 23 may be connected from the gas fuel storage tank GT to the mixer 27 , and the boil-off gas supply line 26 may be connected from the gas fuel storage tank GT to the heat exchanger 16 . .

In this case, the heat exchanger 16 may be provided downstream of the VOC compressor 11 to cool the VOC compressed to about 10 bar with gas fuel, and the temperature of the cooled VOC may be around -20 degrees Celsius. Of course, the temperature and pressure values of the VOC are not limited thereto.

The gas-liquid separator 17 is provided downstream of the heat exchanger 16 to gas-liquid separated cooled VOC, and since the VOC is cooled after the boiling point is increased by compression and transferred to the gas-liquid separator 17, in this embodiment, the VOC is can increase the liquefaction rate of At this time, the gas-liquid separator 17 may recover the LVOC to the oil storage tank OT, and/or deliver it to the VOC storage tank 15 .

The VOC storage tank 15 stores LVOC, which is a liquid VOC separated by the gas-liquid separator 17 after being cooled in the heat exchanger 16 . Of course, when the oil is loaded, the VOC storage tank 15 may also store the SVOC, which is the VOC in the gas phase separated by the gas-liquid separator 17 .

The oil storage tank (OT) can accommodate other crude oil components in addition to the VOC to be volatilized, but since the VOC storage tank 15 stores only the heavy hydrocarbon components volatilized from oil, the VOC storage tank 15 is used to store VOCs. When mixed with gas fuel, control of the supply to the engines ME, GE, DE can be made easier.

A VOC storage line 151 may be connected from the gas-liquid separator 17 to the VOC storage tank 15 , and a VOC supply line 152 may be connected from the VOC storage tank 15 to the mixer 27 . The VOC storage tank 15 may store liquid VOC, and the liquid VOC may be spontaneously vaporized due to factors such as heat penetration from the outside.

In this case, VOC vaporized in the VOC storage tank 15 may flow in the VOC supply line 152 , and the liquid VOC remains in the VOC storage tank 15 and is recovered to the oil storage tank OT if necessary. , may be vaporized through a separate heating source and delivered to the mixer 27 .

The VOC storage tank 15 can receive the low-temperature liquid VOC separated from the gas-liquid separator 17 after being supercooled in the heat exchanger 16, and in this case, additional evaporation in the VOC storage tank 15 is suppressed. The pressure increase inside the VOC storage tank 15 can be minimized.

In this embodiment, gas fuel is delivered to the mixer 27 or supplied to the heat exchanger 16. When the amount of gas fuel supplied to the heat exchanger 16 is reduced, the VOC is less cooled, so the gas-liquid separator 17 The SVOC supplied from the VOC storage tank 15 to the mixer 27 increases.

Conversely, if the amount of gas fuel supplied to the heat exchanger 16 is reduced, the VOC is sufficiently cooled, so that the amount of SVOC supplied to the mixer 27 may be reduced.

That is, in this embodiment, the amount of gas fuel supplied to the heat exchanger 16 can be used to determine the amount of VOC introduced into the mixer 27 , and the flow of gas fuel toward the heat exchanger 16 is, It can be controlled according to the amount of VOC generated in the storage tank OT, the load of the VOC compressor 11, the level of the VOC storage tank 15, internal pressure, and the like.

17 is a conceptual diagram of a VOC processing system according to a fourteenth embodiment of the present invention.

Referring to FIG. 17 , in this embodiment, unlike the thirteenth embodiment, gas fuel heated by VOC in the heat exchanger 16 may be transferred to the mixer 27 . To this end, the gas fuel supply line 23 is connected to the mixer 27 via the heat exchanger 16 .

In this case, the heat exchanger 16 may cool the VOC using liquid gas fuel, and in particular, the heat exchanger 16 may supercool the VOC using the gas fuel and deliver it to the VOC storage tank 15 to be described later. there is. At this time, the heat exchanger 16 may subcool the VOC to about -40 degrees Celsius.

When the VOC is supercooled, there is a fear that hydrate may be generated due to the CO2 contained in the VOC, but this may be resolved as the CO2 in the VOC is removed by the above-described CO2 adsorber 133 .

In this embodiment, liquid gas fuel may be used for cooling (supercooling) of the heat exchanger 16 , and gaseous fuel evaporated in the gas fuel storage tank GT may be connected to the boil-off gas supply line 26 . It can be supplied to other consumers (DEs) such as auxiliary boilers or IGGs.

That is, gaseous fuel having a temperature somewhat higher than that of liquid gaseous fuel may be provided to be consumed without heat exchange with VOC, and VOC may be cooled only by liquid gaseous fuel.

As described above, in this embodiment, since the low-temperature gas fuel discharged from the gas fuel storage tank GT can be heated to VOC, energy used for vaporization of the gas fuel can be reduced.

In addition, in this embodiment, by simultaneously cooling (supercooling) and storing the VOC as LVOC, it is possible to effectively control the mixed flow rate of VOC to match the methane number to ensure engine (ME, GE, DE) operating efficiency.

18 is a conceptual diagram of a VOC processing system according to a fifteenth embodiment of the present invention.

Referring to FIG. 18 , in the VOC processing system 1 according to the fifteenth embodiment of the present invention, the engines ME, GE, and DE to which the VOC is supplied may be limited. As shown in the figure, the engines ME, GE, and DE receiving VOC and gas fuel from the mixer 27 may be a power generation engine GE, etc., and the main engine ME provided for propulsion of the ship S is VOC Gas fuel can be supplied without mixing.

When the main engine (ME) is XDF, the required methane number of the main engine (ME) may be 60MN or more. However, since the methane number of VOC is around 20MN, when VOC is mixed with gas fuel, the methane number of the fuel flowing into the main engine (ME) is insufficient, which may cause a problem.

Of course, in the previous embodiment, the methane number can be adjusted through the CO2 adsorber 133 and the supply of boil-off gas, which is a gas fuel having a high methane number, but considering that the supply amount of VOC is not uniform, the The methane number of a fuel can fluctuate.

Therefore, in this embodiment, in order to prevent the output of the main engine ME from being shaken due to a change in the mixing amount of VOC depending on variables such as the storage amount of oil stored in the oil storage tank OT and the temperature of the route, the main engine ME) allows operation only on gas fuel without VOC mixing.

To this end, the gas fuel supply line 23 and/or the boil-off gas supply line 26 may be branched from the upstream of the mixer 27 and connected to the main engine ME and the power generation engine GE, respectively. That is, the main engine ME is not provided downstream of the mixer 27 , but the power generation engine GE and other demanding parties DE may be disposed.

As such, in this embodiment, the VOC is not mixed with the gas fuel delivered to the main engine (ME), and is supplied only to the power generation engine (GE) and/or other consumers (DE), so that the output of the main engine (ME) is shaken. It is possible to secure the navigational stability of the vessel (S) by suppressing it.

19 is a conceptual diagram of a VOC processing system according to a sixteenth embodiment of the present invention.

Referring to FIG. 19 , in the VOC processing system 1 according to the sixteenth embodiment of the present invention, the VOC compressors 11 are provided in multiple stages, and the intercooler 111 may be disposed between the VOC compressors 11 .

A plurality of VOC compressors 11 may be provided to compress VOCs in multiple stages. In this case, the pressure of the VOCs introduced into the gas-liquid separator 17 may be higher than the pressure in the previous embodiment. Therefore, in the present embodiment, the boiling point of VOC is increased through additional compression of VOC, so that more LVOC can be produced.

The intercooler 111 is provided between the plurality of VOC compressors 11 to cool the VOC. At this time, the refrigerant used by the intercooler 111 to cool the VOC is not limited, and gas fuel may be used as the refrigerant in the intercooler 111 as described in the heat exchanger 16 of the previous embodiment.

In this case, the gas fuel supply line 23 and/or the boil-off gas supply line 26 may be provided to pass through the intercooler 111 in the gas fuel storage tank GT, and then may be connected to the mixer 27 . .

The intercooler 111 may cool the VOC primarily compressed by the VOC compressor 11 with gas fuel or the like, and recover at least a portion of the cooled VOC to the VOC storage tank 15 . At this time, the VOC recovered to the VOC storage tank 15 may be LVOC, and the intercooler 111 may have a structure capable of performing functions of cooling and gas-liquid separation.

A VOC storage line 151 may be connected from the intercooler 111 to the VOC storage tank 15, and the intercooler 111 heats gas fuel and the like with VOC to cool the VOC, and converts liquid VOC from the cooled VOC to VOC. It can be recovered to the storage tank (15).

At this time, the intercooler 111 may suppress the generation of SVOC by supercooling the VOC through the gas fuel and recovering the VOC in a supercooled state in the VOC storage tank 15 as described in the previous heat exchanger 16 .

In addition, the intercooler 111 may recover LVOC, which is at least a part of the cooled VOC, from the VOC storage tank 15 as well as the oil storage tank OT, and for this purpose, from the intercooler 111 to the oil storage tank OT. A VOC recovery line 171 may be connected.

As described above, in this embodiment, the VOC compressor 11 is provided in multiple stages to further increase the recovery rate of LVOC in the gas-liquid separator 17, and the intercooler 111 provided between the VOC compressors 11 can also recover the LVOC. Therefore, it is possible to sufficiently improve the recovery efficiency of VOCs without separately providing a configuration for liquefying VOCs.

20 is a conceptual diagram of a VOC processing system according to a seventeenth embodiment of the present invention.

Referring to FIG. 20 , in the VOC processing system 1 according to the seventeenth embodiment of the present invention, the gas fuel processing unit 20 includes a gas fuel vaporizer 22 , and a heat exchanger 16 and a gas fuel vaporizer ( 22) can be indirectly connected.

The gas fuel vaporizer 22 is provided on the gas fuel supply line 23 connected from the gas fuel storage tank GT to the mixer 27, and heats the gas fuel as a heat medium. The gas fuel vaporizer 22 can heat the gas fuel in liquid (or gaseous phase) discharged from the gas fuel storage tank (GT) by using various types of heat which is not limited, for example, the heat is seawater, steam, It may be glycol water or the like.

To this end, the gas fuel vaporizer 22 may be provided with a heat medium supply unit 221 for supplying heat. The heat supply unit 221 may include a line (not shown) for circulating the heat, a heat pump for pumping the heat (not shown), and a heat heater (not shown).

The heat exchanger 16 which cools the VOC compressed by the VOC compressor 11 can utilize the heat medium of the gas fuel vaporizer 22. As shown in FIG. That is, the heat medium circulation line, one side is connected to the gas fuel vaporizer (22) and the other side is connected to the heat exchanger (16).

At this time, the heat medium may be cooled while heating the gas fuel in the gas fuel vaporizer 22 , and then may be introduced into the heat exchanger 16 to cool the VOC. Therefore, in this embodiment, since the heat medium cooled by the gas fuel can be heated by heat exchange with VOC, the heat medium heater can be omitted or minimized.

Of course, the heat supply unit 221 may appropriately adjust the load of the heat medium heater and/or the flow rate that flows into the heat medium heater in the heat medium circulation line or bypasses the heat medium heater according to the flow rate at which the heat medium is supplied to the heat exchanger 16 .

As such, in this embodiment, energy savings can be realized by utilizing the heat used for vaporization of gas fuel when VOC is cooled.

21 is a conceptual diagram of a ship including a VOC processing system according to an eighteenth embodiment of the present invention.

Referring to FIG. 21 , in the VOC processing system 1 according to the eighteenth embodiment of the present invention, the VOC processing unit 10 includes a VOC pump 154 and a VOC injector 1572 .

The VOC pump 154 pressurizes the VOC generated in the oil storage tank OT. A VOC discharge line 13 may be connected from the oil storage tank OT to the VOC pump 154, and the VOC pump 154 pressurizes the VOC discharged along the VOC discharge line 13 in a gaseous or liquid phase to an appropriate pressure. do.

Alternatively, the present embodiment may use the VOC compressor 11 instead of the VOC pump 154 . That is, since VOC is volatilized in a gaseous state in the oil storage tank (OT) and discharged through the VOC discharge line 13, the VOC discharge line 13 has all configurations capable of increasing the VOC pressure in consideration of the state of VOC. possible.

That is, the VOC pump 154 and the VOC compressor 11 may be provided at once, for example, a gas-liquid separator 17 is disposed in the VOC discharge line 13, and a VOC pump 154 downstream of the gas-liquid separator 17. and the VOC compressor 11 are provided in parallel, and the LVOC separated by the gas-liquid separator 17 may be transferred to the VOC pump 154 , and the SVOC may be transferred to the VOC compressor 11 . For reference, the VOC pump 154 to be described below may be replaced with the VOC compressor 11 or a set of the VOC pump 154 and the VOC compressor 11 .

The VOC injector 1572 returns the pressurized/compressed VOC into the oil storage tank OT. The pressure of the pressurized VOC may be 2 to 10 bar (for example, around 3 bar), and the VOC injector 1572 may return the pressurized VOC in the oil storage tank OT to realize the reduced pressure of the VOC.

In particular, the VOC injector 1572 may inject VOC into the oil storage tank OT in the form of a spray, so that the injected VOC is cooled by reduced pressure to lower the oil temperature in the oil storage tank OT.

That is, the VOC injector 1572 is a spray that sprays the VOC pressurized by the VOC pump 154 or the like into the oil storage tank OT. It can be cooled by the Joule-Thomson effect as it depressurizes. Therefore, the amount of VOC generated in the oil storage tank OT can be suppressed by the VOC being returned and cooled at the same time.

A VOC return line 157 may be connected to the VOC injector 1572 in the VOC pump 154 or the like, and a VOC return valve 1571 may be provided on the VOC return line 157 . The opening degree of the VOC return valve 1571 may be adjusted according to the temperature and/or pressure of the oil stored in the oil storage tank OT.

For example, when it is determined that it is necessary to suppress the amount of VOC generated inside the oil storage tank (OT), the VOC return valve 1571 is sufficiently opened so that the VOC is pressurized through the VOC pump 154 and then by the VOC injector 1572 . It can be sprayed in the oil storage tank (OT).

The VOC discharge line 13 described above is branched from the upstream of the VOC pump 154 and may be connected to a consumer mounted on the vessel S. In this case, the consumer may be a boiler, IGG, etc., and the VOC discharge line 13 may deliver VOC generated in the oil storage tank (OT) to a boiler or the like without pressurization.

To this end, the oil storage tank OT may accumulate VOCs generated therein to increase the internal pressure to the required pressure of the boiler. That is, the VOC return valve 1571 may maintain an unopened state until the pressure inside the oil storage tank OT reaches the required pressure of the boiler or the like.

The oil storage tank OT, for example, may accumulate VOCs generated therein to increase the internal pressure to 2 bar to 3 bar or more. Of course, the internal pressure accumulated in the oil storage tank OT may vary depending on the required pressure of the boiler or the like.

As described above, according to the present embodiment, VOC generated in the oil storage tank OT is suppressed by spraying the VOC generated in the oil storage tank OT into the oil storage tank OT after pressurization.

And/or this embodiment, by increasing the pressure of the oil storage tank (OT) to about 3 bar and supplying the VOC to a boiler or the like in a free flow without compression and consumption, it is possible to simplify the configuration for processing the VOC.

22 to 24 are conceptual diagrams of a ship including a VOC processing system according to a nineteenth embodiment of the present invention, and FIG. 25 is a conceptual diagram of a VOC processing system according to a nineteenth embodiment of the present invention.

22 to 24, the dotted line indicates the VOC discharge line 13, the solid line indicates the VOC return line 157, and the dashed-dotted line indicates the bunkering line BL. .

The VOC treatment system 1 according to the present embodiment may perform VOC recovery at the same time as bunkering by a bunker line BL for a plurality of oil storage tanks OT to block VOC emissions at the source, and also to remove VOCs. There is no need to separately prepare equipment for this. It will be described in detail below.

In this embodiment, the VOC compressor 11 (which can be replaced by the VOC pump 154, of course) pressurizes the VOC generated when the oil is loaded into the oil storage tank OT. In the previous embodiment, the VOC compressor 11 compresses the VOC generated from the oil storage tank OT already loaded with oil, whereas in the present embodiment, VOC compression can be performed simultaneously with bunkering.

Specifically, as shown in FIG. 22 , the VOC compressor 11 compresses the VOC generated in the loading first oil storage tank OT and delivers it to the second oil storage tank OT before loading. Hereinafter, the first and second numbers are assigned according to the bunkering order, but are not limited thereto. In addition, the second oil storage tank OT may mean a third or more, not the second.

In the conventional case, VOC generated in a large amount during bunkering was burned out or consumed unnecessarily.

In this embodiment, the VOC generated in the loading oil storage tank OT is transferred to the empty oil storage tank OT before loading. At this time, as the VOC is compressed by the VOC compressor 11 and then delivered to the empty oil storage tank OT, it is supplied at a pressure higher than the internal pressure of the oil storage tank OT, but the oil storage tank ( OT) is empty, so even if a high pressure VOC is introduced, the VOC can be reduced by volume expansion, so it is not a problem.

As shown in FIG. 23 , the VOC compressor 11 compresses the VOC generated in the second oil storage tank OT when the second oil storage tank OT into which the VOC has already been introduced is loaded and compresses the VOC into the first oil storage tank. (OT) is recovered.

That is, the VOC generated in the loaded oil storage tank (OT) is transferred to the empty oil storage tank (OT), and when loading is performed in the oil storage tank (OT) that has received the VOC, the VOC generated during the loading process is loaded at a certain level. (50 to 80% to the extent that VOC can be sufficiently absorbed while being recovered into the oil) It can be recovered to the over-completed oil storage tank (OT) and/or to another empty oil storage tank (OT).

Unlike the loading of the first oil storage tank OT, the second oil storage tank OT is already filled with VOC. As the oil is loaded, the VOC may be mixed into the oil. For this reason, the amount of VOC generated when the second oil storage tank OT is loaded may be less than the amount generated when the first oil storage tank OT is loaded.

Therefore, since the amount of VOC to be processed is different when the VOC compressor 11 is loaded into the oil storage tank OT after the second time compared to when it is loaded into the oil storage tank OT for the first time, the load or number of operating units is different. can be reduced

VOC generated in the second oil storage tank (OT) is compressed in the VOC compressor (11) and cooled using an intercooler (111), VOC liquefier (14), etc. as necessary, and the first oil storage tank (OT) is recovered into the oil from

That is, the VOC return line 157 connected from the VOC compressor 11 to the inside of the oil storage tank OT is extended to the lower inside of the oil storage tank OT, so that the recovered VOC can be introduced into the oil. . Through this, VOC emission does not occur again after VOC is recovered.

However, in this embodiment, unlike the drawings, as in the embodiment described with reference to FIG. 21 , the VOC return line 157 extends only to the inner upper side of the oil storage tank OT, and extends to the inner lower side of the oil storage tank OT. In order to utilize the bunker line BL, a VOC transfer line (not shown) may be provided from the VOC discharge line 13 to the bunker line BL.

In this case, in order to efficiently control the pressure, flow rate, etc. in the VOC delivery line, the VOC discharge line 13, and the VOC return line 157, the VOC compressor 11 may be provided in the VOC delivery line, but only the VOC discharge Dimensions may be different from those provided on the line 13 .

Of course, unlike the above, the VOC delivery line is provided to branch from the VOC return line 157 downstream of the VOC compressor 11 to which the VOC discharge line 13 is connected, and may share the VOC compressor 11, but is not limited thereto. .

However, in this case, since a part of the bunkering line BL is used for VOC recovery, the oil storage tank OT from which the VOC is recovered into oil may be limited to the one in which bunkering is completed.

In the present embodiment, VOC generated in the last loaded oil storage tank OT may be divided into at least some of the remaining oil storage tanks OT and recovered as shown in FIG. 24 .

The last oil storage tank OT is filled with VOC, and as oil is loaded, it is absorbed by the oil, and some VOCs are recovered/absorbed into the oil loaded in another oil storage tank OT.

Of course, even if it is not the loading of the last oil storage tank (OT), if loading occurs in the new oil storage tank (OT) in a situation where there is one or more oil storage tanks (OT) filled with more than a certain level of oil (the third oil storage tank ( OT), VOC can be distributed and recovered after compression/cooling.

As such, in the present embodiment, there is no process of discharging VOC to the outside even after the loading of all the oil storage tanks OT is finally completed, and oil and LVOC mainly exist inside the oil storage tank OT.

25, in the VOC discharge line 13 and the VOC return line 157 in which the VOC compressor 11 is provided, a pressure gauge (signs not shown), a flow meter (signs not shown), A sensor such as a thermometer (not shown) may be provided, and various valves (not shown) for implementing control of the VOC flow rate may be adjusted by the sensor.

That is, in this embodiment, the VOC continuously generated during shipment is pressurized by the VOC pump 154 or the VOC compressor 11, cooled to an appropriate temperature, and then transferred to an empty oil storage tank (OT) that has not yet been loaded. After dividing and moving, the transferred VOC is injected into the lower part of the oil storage tank (OT) where an appropriate amount is loaded, and the VOC is reabsorbed into the oil.

In this embodiment, by repeating this process, all VOCs generated between shipments are finally absorbed in the oil at the end of shipment. By blocking the emission of VOCs at the source, it is possible to respond to environmental regulations and reduce OPEX. .

26 is a conceptual diagram of a ship including a VOC processing system according to a twentieth embodiment of the present invention.

Referring to Figure 26, the VOC treatment system 1 according to the twentieth embodiment of the present invention, when supplying the VOC to the engines (ME, GE), the methane number of the VOC (methane number) of the engines (ME, GE) The exhaust of the engine (ME, GE) can be utilized in case the condition is not met.

A turbocharger 50 is provided in the engines ME and GE of this embodiment. In the turbocharger 50, the compression unit 50a and the turbine unit 50b are connected by a common shaft, and when the turbine unit 50b rotates by exhaust, the compression unit 50a rotates to compress scavenging air. am.

At this time, the scavenging air supply line 51 is connected to the intake manifolds of the engines (ME, GE) via the compression unit (50a), and, conversely, from the exhaust manifolds of the engines (ME, GE) via the turbine unit (50b). An exhaust discharge line 52 may be provided.

As described above, for engines (ME, GE) in which the turbocharger 50 is provided, an exhaust gas recirculation system (EGR) recirculating exhaust gas into a cylinder in order to lower the ratio of nitrogen oxides included in exhaust gas due to recent environmental regulations. gas recirculation) is used.

This exhaust gas recirculation system is configured to supply exhaust containing inert gas (carbon dioxide) together with scavenging air into the cylinder to reduce the combustion temperature in the cylinder to suppress the generation of nitrogen oxides.

Such an exhaust gas recirculation system may also be applied to this embodiment, and in this embodiment, the exhaust gas recirculation system may be referred to as an exhaust circulation unit 53 .

The exhaust circulation unit 53 of this embodiment may supply exhaust from before and after the turbine unit 50b before and after the compression unit 50a to be mixed with scavenging air, for example, in the upstream of the turbine unit 50b. High-pressure exhaust circulation (HP EGR) for supplying high-pressure exhaust to the upstream or downstream of the compression unit 50a or low-pressure exhaust circulation (LP) for supplying low-pressure exhaust from the downstream of the turbine unit 50b to the upstream of the compression unit 50a EGR) and the like.

To this end, the low-pressure exhaust circulation line 531 is connected from the downstream of the turbine part 50b to the upstream or downstream of the compression part 50a, while from the upstream of the turbine part 50b to the upstream or downstream of the compression part 50a. High-pressure exhaust circulation lines 531 and 532 may be connected, and a cooler (not shown), a filter (not shown), an exhaust recirculation valve 54 (EGR valve), etc. may be connected to each of the exhaust circulation lines 531 and 532 . will be prepared

Some of the exhaust circulating through the exhaust circulation unit 53 may join the VOC through the exhaust transmission lines 531a and 532a, which will be described later.

In this embodiment, a VOC discharge line 13 may be provided from the oil storage tank OT to the engines ME and GE in order to supply VOC generated from the oil storage tank OT to the engines ME and GE. In addition, the VOC discharge line 13 is provided with a VOC compressor 11 , a mixer 56 , and the like.

VOC generated from the oil storage tank (OT) has a calorific value, so it can be used as fuel for the engine (ME, GE), but the type of engine (ME, GE) (main engine (ME, GE), power generation engine (ME, GE), etc.) or the load of the engine (ME, GE), the operating conditions, etc., the fuel condition required by the engine (ME, GE) may vary. will have a major impact on

In order to maintain stable operation while operating the engines (ME, GE) in gas mode, the methane number must be secured above a certain level. Since it is impossible to control the methane number when only VOC is supplied, liquefied gas and the like were mixed in the previous embodiment.

However, in this embodiment, instead of separately mixing the liquefied gas or in addition to mixing the liquefied gas, an inert gas (carbon dioxide) can be used to efficiently control the methane number, especially considering that the exhaust contains a large amount of carbon dioxide, By mixing exhaust with VOC, the methane number of VOC supplied to engines (ME, GE) can be adjusted.

To this end, a mixer 56 is provided between the oil storage tank (OT) and the engine (ME, GE) (for example, between the VOC compressor 11 and the engine (ME, GE)), exhaust circulation lines (531, 532) exhaust delivery lines 531a and 532a are connected to the mixer 56 from At least a portion of the circulating exhaust may be mixed with VOC to adjust the methane number of the VOC and supply it to the engines (ME, GE).

Specifically, the exhaust transmission lines 531a and 532a include a low-pressure exhaust transmission line 531a branched from the low-pressure exhaust circulation line 531 or a high-pressure exhaust transmission line 532a branched from the high-pressure exhaust circulation lines 531 and 532. The exhaust delivery valve 55 provided in the exhaust delivery lines 531a and 532a may adjust the mixed flow rate of the exhaust according to the engine (ME, GE) state and the methane number of the VOC.

That is, the exhaust delivery valve 55 may adjust the delivery flow rate of the exhaust so that the methane number meets the requirements of the engines (ME, GE) as the exhaust including carbon dioxide is mixed with the VOC, and for this, the temperature or flow rate of the exhaust is adjusted. Sensors to detect, methane number of VOC, engine (ME, GE) requirement information reception configuration, etc. may be added as much as possible.

As described above, in this embodiment, when VOC is compressed and supplied to the engines (ME, GE), but a methane number above a certain level is required to operate the engines (ME, GE) in gas mode, at least among the exhaust (carbon dioxide) circulating in the scavenging air By mixing a portion of VOC with VOC to adjust the methane number, it is possible to control the methane number even without liquefied gas mixing, making it possible to construct a simple and efficient system.

27 is a conceptual diagram of a ship including the VOC processing system according to the twenty-first and twenty-second embodiments of the present invention.

Referring to FIG. 27 , the VOC processing system 1 according to the twenty-first embodiment of the present invention mixes the VOC and liquefied gas stored in the VOC storage tank 15 and the gas fuel storage tank GT, respectively, and the engine ME , GE, DE) includes a fuel processing unit (10, 20), a gas analyzer 232, and a control unit 30 for supplying the fuel. Hereinafter, the present embodiment will be mainly described on the points that are different from the previous embodiment 5, and the parts omitted from the description will be replaced with the previous content.

The fuel processing units 10 and 20 may satisfy the methane number required for each load in the engines ME, GE, and DE by mixing the liquefied gas with the VOC in an appropriate ratio to prevent smooth combustion and knocking.

To this end, the fuel processing units 10 and 20 may include a VOC processing unit 10 covering components used to process VOC, and a gas fuel processing unit 20 covering components used for processing gas fuel. there is.

The VOC processing unit 10 supplies VOC generated from the oil storage tank OT as fuel of the engines ME, GE, and DE mounted on the ship S. To this end, the VOC processing unit 10 may include a VOC compressor 11 , a third heat exchanger 16c , a gas-liquid separator 17 , and the like.

The third heat exchanger 16c cools the VOC supplied through the VOC supply line 152 at the rear end of the VOC compressor 11 with seawater supplied through the seawater pump 40, and converts the heat-exchanged VOC to a gas-liquid separator 17 . can be supplied with The stored seawater may be supplied through a seawater supply line using the seawater pump 40, and may be discharged as seawater after use. A thermometer may be provided in the VOC supply line 152 at the rear end of the third heat exchanger 16c to verify whether the temperature of the heat-exchanged VOC corresponds to the temperature required by the engines ME, GE, and DE.

The gas-liquid separator 17 may supply a portion of the VOC liquefied through heat exchange in the third heat exchanger 16c to the oil storage tank OT through the VOC recovery line 171, and supply the remaining VOC to the VOC supply line ( 152) through the engine (ME, GE, DE) can be supplied. At this time, at the rear end of the gas-liquid separator 17 connected to the engine (ME, GE, DE), a filter (not shown) is disposed upstream of the mixing point of VOC and liquefied gas to remove impurities contained in VOC. there is. In this case, a portion of VOC upstream of the filter may be supplied to the oil storage tank OT through the VOC recovery line 171 .

The gas fuel processing unit 20 may mix the liquefied gas of the gas fuel storage tank GT with the VOC supplied to the engines ME, GE, and DE through the VOC supply line 152 . A material in which VOC and liquefied gas are mixed in the gas fuel processing unit 20 may be referred to as a fuel in the present specification.

A gas fuel supply line 23 may be provided from the gas fuel processing unit 20 to the engines ME, GE, and DE, and in the gas fuel supply line 23, the pressure of the fuel is transferred from the engines ME, GE, and DE. A pressure gauge 233 may be provided to verify whether the pressure corresponds to a required pressure.

Gas analyzer 232, VOC supplied to the engines (ME, GE, DE) through the VOC processing unit 10, and the methane number before the liquefied gas mixed with the VOC through the gas fuel processing unit 20 is mixed with each other, respectively measure As described above, in the present specification, the methane number may be interpreted as encompassing all fuel specifications such as fuel components or calorific values in addition to the methane number.

The control unit 30 controls the flow rate of VOC and/or liquefied gas delivered to the mixing point of VOC and liquefied gas according to the methane value measured by the gas analyzer 232 in the gas fuel processing unit 20 . Accordingly, the ratio of VOC and liquefied gas included in the fuel generated by the gas fuel processing unit 20 may be adjusted by the control unit 30 .

The control unit 30 may control the flow rate of VOC and/or liquefied gas delivered to the gas fuel processing unit 20 in various ways using a pump, a valve, or the like. For example, any one or more of the VOC processing unit 10 and the gas fuel processing unit 20 may be provided with a delivery valve for controlling the flow rates of VOC and liquefied gas, respectively, and the control unit 30 controls the flow rate of the delivery valve. can be adjusted Preferably, a pressure regulating valve 234a may be provided on the VOC supply line 152 of the VOC processing unit 10 and/or the gas fuel supply line 23 of the gas fuel processing unit 20, respectively, and the control unit ( 30) may adjust the pressure of the pressure control valve 234a.

At this time, the control unit 30 controls the transfer valve, preferably the pressure control valve 234a, according to the measured value of the gas analyzer 232, thereby controlling the methane number of the fuel generated by the gas fuel processing unit 20 to the engine (ME, It can be adjusted to the level required by GE, DE).

Upstream of the mixing point of VOC and liquefied gas, a VOC return line (not shown) for returning at least a portion of the VOC to the VOC storage tank 15 may be provided. In this case, a VOC return valve (not shown) serving as a return valve may be provided on the VOC return line (not shown).

Also, in the gas fuel supply line 23 in the same/similar manner, there is a gas fuel return line (not shown) that returns at least a portion of the liquefied gas discharged from the gas fuel storage tank (GT) upstream of the mixing point of VOC and liquefied gas. A gas fuel return valve (not shown) as a return valve may be provided on the gas fuel return line (not shown).

In this case, the control unit 30 controls the VOC return valve (not shown) and/or the gas fuel return valve (not shown) according to the measured value of the gas analyzer 232 , to thereby control the VOC return valve (not shown). By adjusting the flow rate of VOC delivered to the engine (ME, GE, DE) and/or the flow rate of liquefied gas delivered to the engine (ME, GE, DE) by the gas fuel return valve (not shown), The methane number of the fuel can be tailored to the engine (ME, GE, DE).

Therefore, the control unit 30 may measure the methane number of the VOC and the liquefied gas before mixing the VOC and the liquefied gas, respectively, to actively control the flow rate at which the VOC and the liquefied gas are mixed.

As described above, in this embodiment, the VOC, which was thrown into the atmosphere, is used as a fuel for the engine (ME, GE, DE), but the fuel specifications (methane number, calorific value, component, etc.) required by the engine (ME, GE, DE) are By mixing liquefied gas with VOC and supplying it to engines (ME, GE, DE) to satisfy the needs, VOCs can be reused while ensuring engine (ME, GE, DE) operating efficiency.

Referring to FIG. 27 , in the VOC treatment system 1 and the VOC treatment method using the same according to the twenty-second embodiment of the present invention, in the VOC treatment system 1 according to the twenty-first embodiment, the methane number of VOC and liquefied gas A specific structure for measuring each , and a control method of the controller 30 using the same are provided. Hereinafter, the present embodiment will be mainly described on the points that are different from the previous embodiment 21, and the parts omitted from the description will be replaced with the previous content.

The control unit 30 controls the flow rate of VOC and/or liquefied gas delivered to the mixing point of VOC and liquefied gas according to the methane value measured by the gas analyzer 232 in the gas fuel processing unit 20 . That is, the control unit 30 controls the mixing ratio of VOC and liquefied gas.

The gas analyzer 232 may measure the methane number of the VOC and the liquefied gas using gas chromatography, but it takes time to measure. Therefore, when the environmental change of the system is accompanied, such as a sudden change in the load of the engine (ME, GE, DE), there may be a delay in controlling the VOC and liquefied gas mixture ratio through the methane number measurement, and measures to reduce or prevent it this is required

In the present embodiment, it is possible to reduce or prevent a delay that may occur when controlling the mixing ratio of VOC and liquefied gas by storing and utilizing each methane number as a reference value before mixing of VOC and liquefied gas.

Before mixing VOC and liquefied gas, measure the methane number, respectively, and set the reference value. When measuring the methane number of VOC and liquefied gas, respectively, VOC is upstream of the mixing point of VOC and liquefied gas, and the methane number is measured downstream of the gas-liquid separator 17, and the liquefied gas is upstream of the mixing point of VOC and liquefied gas Measure the methane number in

Methane values of VOC and liquefied gas are measured periodically, preferably at intervals of several minutes to several hours, and stored in the control unit 30 as reference values for each of VOC and liquefied gas.

The control unit 30 calculates the methane number change of each of VOC and liquefied gas according to the system environment change based on the stored reference value to satisfy the specifications of fuel required by the engines (ME, GE, DE) and VOC and Calculate the mixing ratio of the liquefied gas. Through this, the control unit 30 controls the flow rate of VOC and/or liquefied gas delivered to the mixing point of VOC and liquefied gas.

As such, in this embodiment, in order to reduce or prevent a delay that may occur when controlling the mixing ratio of VOC and liquefied gas, VOC is upstream of the mixing point of VOC and liquefied gas, and the methane number is measured downstream of the gas-liquid separator 17 The liquefied gas measures the methane number upstream of the mixing point of VOC and liquefied gas and stores the reference value. By calculating the VOC and liquefied gas mixing ratio, it is possible to quickly control the mixing ratio.

28 is a conceptual diagram of a VOC processing system according to a twenty-third embodiment of the present invention.

Referring to FIG. 28 , the VOC processing system 1 according to the twenty-third embodiment of the present invention is similar to the first embodiment described with reference to FIG. 2 or the twelfth embodiment described with reference to FIG. 15, a gas fuel storage tank ( GT) liquefied gas is mixed with VOC generated in the oil storage tank (OT) and supplied to the main engine (ME).

To this end, in this embodiment, a gas fuel supply line 23 for delivering liquefied gas from the gas fuel storage tank GT to the engines ME, GE, and DE is provided, and from the oil storage tank OT to the engine ME, A VOC discharge line 13 for delivering VOC to GE, DE) may be provided, and a mixer 27 for mixing VOC and liquefied gas may be provided.

At this time, the gas fuel supply line 23 is provided with a gas fuel vaporizer 22 for vaporizing the liquefied gas discharged from the gas fuel storage tank GT through the gas fuel pump 21, and the gas fuel supply line 23 is It can be connected to the main engine ME, etc. so that the main engine ME consumes only the liquefied gas among the liquefied gas and the VOC to operate. Alternatively, the gas fuel supply line 23 may be branched downstream of the gas fuel vaporizer 22 , and one side may be connected to the main engine ME and the other side may be connected to the mixer 27 through which the VOC exhaust line 13 passes.

Therefore, the liquefied gas discharged from the gas fuel storage tank GT may be introduced into the main engine ME along the gas fuel supply line 23 connected to the main engine ME, or the like, or to the mixer 27 After being introduced and mixed with VOC, it may be consumed by the main engine ME along the gas fuel supply line 23 connected to the main engine ME through the VOC discharge line 13 .

That is, in this embodiment, in addition to the VOC processing unit 10 that compresses the VOC generated in the oil storage tank OT provided in the ship S and supplies it to the engines ME, GE, and DE mounted on the ship S, , includes a gas fuel processing unit 20 for mixing the liquefied gas of the gas fuel storage tank GT provided in the ship S with the VOC supplied to the engines ME, GE, DE.

Therefore, in this embodiment, as in the previous embodiment, in preparation for failing to meet the fuel specifications required by the engines (ME, GE, DE) with only VOC, liquefied gas is mixed with VOC to adjust the methane number, etc. will do

However, the gas fuel storage tank (GT) is a membrane type or independent type Type B that stores liquefied gas at atmospheric pressure. Even in the case of Type C, which stores liquefied gas, the amount of BOG can be reduced, but it cannot be completely blocked, so it may be desirable to discharge BOG.

Therefore, the gas fuel processing unit 20 of the present embodiment may discharge the boil-off gas generated in the gas fuel storage tank GT to the outside. At this time, the discharged BOG may be delivered to the main engine ME or the like through the BOG supply line 26 and consumed as described in the twelfth embodiment of FIG. 15 .

However, in order to deliver the boil-off gas generated from the gas fuel storage tank (GT) to the engines (ME, GE, DE), etc., it is necessary to provide a compressor for boil-off gas. However, in the present embodiment, instead of providing a separate BOG compressor in the BOG supply line 26 , the VOC compressor 11 provided in the VOC discharge line 13 may be used for BOG.

That is, in this embodiment, the boil-off gas supply line 26 joins the upstream of the VOC compressor 11 from the VOC discharge line 13 to deliver the boil-off gas generated from the gas fuel storage tank GT to the VOC compressor 11 . can Therefore, in the present embodiment, when the BOG is discharged for maintaining the internal pressure of the gas fuel storage tank (GT), the BOG compressor is not separately provided, but the VOC compressor 11 can be substituted for the BOG compressor. Through this, the present embodiment omits the compressor for BOG, so that it can occupy an advantageous position in manufacturing cost as well as operating cost, maintenance cost, installation space, and the like.

As such, the gas fuel processing unit 20 of this embodiment discharges the boil-off gas generated in the gas fuel storage tank GT to suppress the increase in the internal pressure of the gas fuel storage tank GT, but to the VOC before compression in the VOC processing unit 10 It is transmitted, mixed with the VOC, and then compressed by the VOC compressor 11 .

However, in this case, based on the junction of the VOC discharge line 13 and the boil-off gas supply line 26 upstream of the VOC compressor 11, upstream of each of the VOC discharge line 13 and the boil-off gas supply line 26 Non-return valves 134 and 261 may be provided. This prevents the BOG discharged from the gas fuel storage tank (GT) from being transferred to the oil storage tank (OT) and, conversely, prevents the VOC discharged from the oil storage tank (OT) from being transferred to the gas fuel storage tank (GT). can

As such, in this embodiment, the liquefied gas of the gas fuel storage tank (GT) is mixed with VOC generated in the oil storage tank (OT) and supplied to the main engine (ME) for consumption, but discharged from the gas fuel storage tank (GT) It is possible to control the internal pressure of the gas fuel storage tank (GT) by discharging the boil-off gas and delivering it to the VOC compressor 11 and using the VOC compressor 11 to process the VOC.

29 is a conceptual diagram of a VOC processing system according to a twenty-fourth embodiment of the present invention.

Referring to FIG. 29 , the VOC treatment system 1 according to the twenty-fourth embodiment of the present invention compresses the VOC generated in the oil storage tank OT, similarly to the previous embodiment, and the engine (ME, GE) and a VOC processing unit 10 supplied to the gas fuel storage tank GT, and a gas fuel processing unit 20 that mixes the liquefied gas (including evaporated gas) of the gas fuel storage tank (GT) with the VOC supplied to the engines (ME, GE), and a control unit (30) may be included.

In addition, in the present embodiment, the mixer 27 is provided upstream of the VOC compressor 11 so as to mix the liquefied gas with the VOC to be introduced into the VOC compressor 11 provided in the VOC processing unit 10. It is similar to the embodiment (of course, the embodiment can be modified in which liquefied gas is mixed downstream of the VOC compressor 11).

However, this embodiment may further include an additional configuration compared to the previous embodiments from a control point of view, and below, the differences between the present embodiment will be mainly described.

In this embodiment, the control unit 30 monitors the VOC (especially the flow rate) supplied to the engines ME and GE, and can control the flow rate of the liquefied gas delivered to the VOC by the gas fuel processing unit 20 . Specifically, the control unit 30 compares and analyzes the load of the engine (ME, GE) and the flow rate of VOC in the gas phase supplied to the engine (ME, GE) by the gas-liquid separator (17), and the gas fuel processing unit (20) By controlling the flow rate of liquefied gas delivered to the VOC through the engine (ME, GE), it is possible to control the VOC in the gas phase flowing into the engine (ME, GE) to match the load of the engine (ME, GE).

VOC generated in the oil storage tank (OT) is mixed with the liquefied gas of the gas fuel storage tank (GT) in the mixer 27, compressed by the VOC compressor 11, and a heat exchanger 16 using seawater, etc. After roughing, it is separated into a gaseous VOC and a liquid VOC by the gas-liquid separator 17 .

At this time, the liquid VOC may be stored in the VOC storage tank 15 through the VOC storage line 151 and later delivered to other consumers (DE) through the VOC supply line 152 or the like, or may be vented to the outside. On the other hand, VOC in the gas phase is supplied to the engines (ME, GE).

That is, in the process of compressing and cooling the VOC discharged from the oil storage tank OT and supplying it to the engines ME and GE, the liquid VOC may be excluded from the flow rate supplied to the engines ME and GE.

In this case, there may be a situation where the flow rate of VOC in the gas phase is not sufficient compared to the flow required by the engine (ME, GE). Therefore, it may be necessary to supplement the VOC in the gas phase with the liquefied gas of the gas fuel storage tank (GT). there is.

To this end, in the present embodiment, in addition to the upstream mixer 27 for mixing liquefied gas with VOC upstream of the VOC compressor 11, the gas-liquid separator 17 is liquefied into the VOC separated by the gas-liquid separator 17 downstream. A downstream mixer 27 for mixing the gas may be further provided.

And/or in this embodiment, the control unit 30 monitors the VOC flow rate upstream of the mixer 27 provided downstream of the gas-liquid separator 17, and the flow rate of the liquefied gas delivered to the VOC by the gas fuel processing unit 20 can be controlled.

That is, in this embodiment, in order to prepare for the possibility that the VOC in the gas phase may be insufficient compared to the required amount of the engine (ME, GE), the liquefied gas is directly supplemented to the VOC in the gas phase, or the liquefaction mixed with the VOC in the gas-liquid separator 17 upstream. By controlling the flow rate of gas, it is possible to change the flow rate of VOC in the gas phase.

Since liquefied gas (especially boil-off gas) is mostly methane, when liquefied gas is mixed with VOC, VOC in liquid phase that is liquefied in the process of being compressed by the VOC compressor 11 and cooling in the heat exchanger 16 can be reduced. there will be This means that the flow rate of VOC in the gas phase separated from the gas-liquid separator 17 by mixing of the liquefied gas can be increased.

Therefore, in this embodiment, the liquefied gas is mixed with the VOC generated in the oil storage tank (OT), while monitoring the flow rate of the VOC in the gas phase between the gas-liquid separator 17 and the engine (ME, GE), the mixing amount of the liquefied gas to control Through this, in the present embodiment, the load of the engines ME and GE can be stably maintained by adjusting the flow rate of the VOC of the gas phase separated from the gas-liquid separator 17 .

For reference, the control of the flow rate of the liquefied gas in this embodiment may be used in various ways, such as controlling using a valve or controlling using the number of returning some of the liquefied gas flowing in one direction.

And/or this embodiment may implement a control in which the control unit 30 increases the compression efficiency of the VOC compressor 11 and protects the VOC compressor 11 . Specifically, the control unit 30 sets a dew point threshold value of the VOC for the VOC compressor 11 . In this case, the setting includes not only a case determined by a separate input, but also a case automatically determined by the VOC compressor 11 or the like.

In a state in which the dew point threshold value is set, the control unit 30 monitors the dew point of the VOC sucked into the VOC compressor 11 . In this case, the monitoring may be implemented by measuring the temperature of VOC, but any other method capable of identifying the dew point may be freely used.

The control unit 30 may control the flow rate of the liquefied gas delivered to the VOC by the gas fuel processing unit 20 based on the monitoring result. At this time, the control unit 30 is controlled by the gas fuel processing unit 20 to the mixer 27 by the gas fuel processing unit 20 so that the dew point of the VOC mixed with the liquefied gas in the mixer 27 provided upstream of the VOC compressor 11 is maintained below the dew point limit value. Controls the flow rate of the inflow liquefied gas.

Since the VOC generated in the oil storage tank (OT) has a relatively high dew point, the VOC compressor 11 must be designed to withstand high temperature in the process of pressurizing the VOC to a pressure that can supply the engine (ME, GE). there is This leads to a significant increase in the installation cost and operating cost of the VOC compressor 11 , and thus causes a problem of impairing the efficiency of system operation.

Therefore, in this embodiment, in consideration of the characteristics of VOC having a high dew point, liquefied gas is mixed with VOC generated in the oil storage tank (OT) to lower the dew point by a significant amount, so that the high temperature VOC compressor 11 can withstand high temperature. It is possible to reduce the CAPEX by eliminating the need to provide

That is, the control unit 30 of this embodiment appropriately mixes the liquefied gas with the VOC flowing into the VOC compressor 11 to lower the dew point, thereby lowering the temperature environment in the VOC compressor 11 to meet the design specifications of the VOC compressor 11 . can be lowered.

The control of the controller 30 based on this dew point may be implemented by replacing the concentration of _{hydrogen sulfide (H 2 S).} That is, the control unit 30 monitors the hydrogen sulfide concentration of the VOC flowing into the VOC compressor 11 and mixes the liquefied gas according to the result, so that the VOC hydrogen sulfide concentration is maintained within a limit value.

Of course, this embodiment informs that the concentration of a specific substance that is included in the VOC in addition to hydrogen sulfide and desired to be monitored can be freely utilized for the control of the control unit 30 .

As such, in this embodiment, in order to prepare for a case where the VOC flow rate of the gas phase to be introduced into the engine (ME, GE) is insufficient in the process of supplying the VOC to the engine (ME, GE) after gas-liquid separation, the liquefied gas mixture flow rate is adjusted. It is possible to appropriately control the VOC flow rate in the gas phase. In addition, the present embodiment can improve the design requirements of the VOC compressor 11 by adjusting the flow rate of the liquefied gas mixed with the VOC upstream of the VOC compressor 11 to lower the dew point of the VOC.

The present invention encompasses all embodiments generated by a combination of at least one embodiment and known technology, or a combination of at least two or more embodiments, in addition to the embodiments described above.

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

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

S: Ship OT: Oil storage tank
GT: Gas fuel storage tank ME: Main engine
GE: power generation engine, auxiliary engine DE: other customers
1: VOC processing system 10: VOC processing unit
11: VOC compressor 11a: first VOC compressor
11b: second VOC compressor 111: intercooler
12: reformer 13: VOC discharge line
13a: first VOC emission line 13b: second VOC emission line
13c: third VOC discharge line 131: flow meter
132: pressure gauge 133: CO2 adsorber
134: non-return valve 14: VOC liquefier
15: VOC storage tank 151: VOC storage line
152: VOC supply line 153: pressure gauge
154: VOC pump 155: auxiliary tank
156: flow meter 157: VOC return line
1571: VOC return valve 1572: VOC injector
158: VOC high pressure pump 159: VOC vaporizer
16: heat exchanger 16a: first heat exchanger
16b: second heat exchanger 16c: third heat exchanger
17: gas-liquid separator 17a: first gas-liquid separator
17b: second gas-liquid separator 171: VOC recovery line
20: gas fuel processing unit 21: gas fuel pump
22: gas fuel vaporizer 221: heat supply unit
23: gas fuel supply line 231: flow meter
232: gas analyzer 233: pressure gauge
234a, 234b: pressure control valve 235: gas fuel return line
236: gas fuel return valve 24: gas fuel high pressure pump
25: gas fuel branch line 251: gas fuel heater
252: pressure control valve 26: boil-off gas supply line
261: non-return valve 27: mixer
28: gas fuel liquefier 30: control unit
40: sea water pump 50: turbocharger
50a: compression part 50b: turbine part
51: scavenging air supply line 52: exhaust discharge line
53: exhaust circulation unit 531: low pressure exhaust circulation line
531a: low pressure exhaust delivery line 532: high pressure exhaust circulation line
532a: high pressure exhaust delivery line 54: exhaust recirculation valve
55: exhaust delivery valve 56: mixer

Claims (7)

a VOC processing unit for compressing VOC generated in an oil storage tank provided on a ship and supplying it to an engine mounted on the ship; and
and a gas fuel processing unit for mixing the liquefied gas of the gas fuel storage tank provided in the ship with the VOC supplied to the engine,
The VOC processing unit,
Having a gas-liquid separator that separates VOC mixed with liquefied gas into a gaseous phase and a liquid phase and supplies the separated gaseous VOC to the engine,
Monitoring the VOC of the gas phase supplied to the engine by the gas-liquid separator, further comprising a control unit for controlling the flow rate of the liquefied gas delivered to the VOC by the gas fuel processing unit,
The VOC processing unit,
A VOC compressor for compressing the VOC discharged from the oil storage tank,
The gas fuel processing unit,
The VOC processing system, characterized in that the BOC generated in the gas fuel storage tank is transferred from the VOC processing unit to the VOC upstream of the VOC compressor without additional compression. According to claim 1, wherein the control unit,
The VOC processing system, characterized in that by analyzing the load of the engine and the flow rate of VOC in the gas phase supplied to the engine by the gas-liquid separator, the flow rate of the liquefied gas delivered to the VOC by the gas fuel processing unit is controlled. According to claim 1, wherein the VOC processing unit,
Further comprising a mixer provided upstream of the VOC compressor to mix the liquefied gas with the VOC,
The control unit is
VOC processing system, characterized in that for controlling the flow rate of the liquefied gas delivered to the mixer by the gas fuel processing unit. According to claim 1, wherein the VOC processing unit,
Further comprising a mixer provided downstream of the gas-liquid separator to mix the liquefied gas with the VOC of the gas phase separated in the gas-liquid separator,
The control unit is
VOC treatment system, characterized in that by monitoring the VOC upstream of the mixer to control the flow rate of the liquefied gas delivered to the VOC by the gas fuel processing unit. a VOC processing unit for compressing VOC generated in an oil storage tank provided on a ship and supplying it to an engine mounted on the ship; and
and a gas fuel processing unit for mixing the liquefied gas of the gas fuel storage tank provided in the ship with the VOC supplied to the engine,
The VOC processing unit,
and a VOC compressor for compressing the VOC discharged from the oil storage tank,
A control unit that sets a dew point limit value of VOC for the VOC compressor, monitors the dew point of VOC sucked into the VOC compressor, and controls the flow rate of liquefied gas delivered to VOC by the gas fuel processing unit; includes,
The VOC processing unit,
A VOC compressor for compressing the VOC discharged from the oil storage tank,
The gas fuel processing unit,
The VOC processing system, characterized in that the BOC generated in the gas fuel storage tank is transferred from the VOC processing unit to the VOC upstream of the VOC compressor without additional compression. The method of claim 5, wherein the VOC processing unit,
Further comprising a mixer provided upstream of the VOC compressor to mix the liquefied gas with the VOC,
The control unit is
VOC processing system, characterized in that for controlling the flow rate of the liquefied gas delivered to the VOC by the gas fuel processing unit so that the dew point of the VOC mixed with the liquefied gas in the mixer is maintained below the dew point threshold value. A ship having the VOC treatment system according to any one of claims 1 to 6.

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