KR101741834B1 - Apparatus for recovering VOC - Google Patents

Abstract

The present invention provides an apparatus for recovering volatile organic compounds (VOCs) which is designed to maximally utilize available energy while controlling the discharge of VOCs to the atmosphere. The apparatus for recovering VOCs comprises the following: a first compressor compressing oil mist supplied from a crude oil storage tank; a first heat exchanger cooling high pressure fluid passed through the first compressor; an expansion valve decompressing the high pressure fluid passed through the first heat exchanger, or first gas separated from the high pressure fluid using a pre-processing unit; and a gas-liquid separator separating the high pressure fluid or the first gas passed through the expansion valve into second gas and second liquid, and supplying the second gas to a combustor and supplying the second liquid to a storage tank.

Description

[0001] Apparatus for recovering VOC [0002]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an apparatus for recovering volatile organic compounds, and more particularly, to a volatile organic compound recovery apparatus designed to suppress the emission of volatile organic compounds generated in a crude oil storage tank or the like and utilize available energy as much as possible .

Volatile organic compounds (VOCs) are organic compounds that evaporate easily due to their low boiling point, and they contain various kinds of components depending on their origin. Volatile organic compounds may be toxic or odorous and may contain flammable components. If the volatile organic compounds are released into the atmosphere, they will pollute the atmosphere.

Fossil fuels such as crude oil are also sources of volatile organic compounds. Volatile organic compounds are excessively generated in crude oil carriers and the like that transport large amounts of such crude oil. Volatile organic compounds are particularly common during shipment or unloading of liquid cargoes, such as crude oil, and may be generated inside the tank to increase pressure during transport of crude oil. Therefore, more effective treatment of such volatile organic compounds is required.

However, in the conventional case, it is limited to a treatment method of simply discharging it or storing it in a separate refrigerant and storing it, and the discharge amount is reduced by controlling the storage pressure of the liquid cargo, but it has not been effective. In particular, when the volatile organic compound is liquefied, the efficiency is not high and the energy is wasted, and the uncompensated residue is released into the atmosphere, leading to contamination. In addition, despite the availability of volatile organic compounds (VOCs), there is a focus on the disposal method of reducing emissions or discharging more safely, which is very inefficient in terms of energy efficiency.

Korean Patent Publication No. 10-2008-0097148, (2008.11.04)

Disclosure of Invention Technical Problem [8] The present invention provides a volatile organic compound recovery apparatus designed to suppress emission of volatile organic compounds generated in a crude oil storage tank and utilize available energy as much as possible.

The technical problem of the present invention is not limited to the above-mentioned problems, and other problems not mentioned can be clearly understood by those skilled in the art from the following description.

The apparatus for recovering a volatile organic compound according to the present invention comprises a first compressor for compressing a vapor supplied from an oil storage tank, a first heat exchanger for cooling a high-pressure fluid passing through the first compressor, A high pressure fluid or an expansion valve for decompressing a first gas separated from the high pressure fluid through a preprocessing unit, a high pressure fluid which has passed through the expansion valve, or the first gas is separated into a second gas and a second liquid, And a gas-liquid separator for supplying the second gas to the combustion engine and supplying the second liquid to the storage tank.

And a second heat exchanger disposed between the first heat exchanger and the expansion valve and separating the second gas separated from the gas-liquid separator from the high-pressure fluid or the first gas.

And a third heat exchanger disposed between the second heat exchanger and the expansion valve for exchanging heat between the second liquid separated from the gas-liquid separator and the high-pressure fluid or the first gas.

The pre-treatment unit may further include a pretreatment separator provided between the first heat exchanger and the second heat exchanger, for separating the first gas from the high-pressure fluid and providing the first gas to the second heat exchanger.

The pretreatment unit may further include a moisture removing unit installed between the first heat exchanger and the pretreatment separator or between the pretreatment separator and the second heat exchanger.

The pretreatment unit may further include a second compressor installed between the pretreatment separator and the second heat exchanger to pressurize the first gas.

And a fourth heat exchanger installed between the second compressor and the second heat exchanger to cool the first gas.

And a high-pressure tank connected to the branch pipe and storing the first gas. The high-pressure tank may further include a high-pressure tank connected to the branch pipe and branched from the pipeline through which the first gas flows between the second compressor and the gas-liquid separator.

And a pressure reducing valve formed in the branch pipe to adjust a pressure of the first gas introduced into the high pressure tank.

And an evaporator installed between the first heat exchanger and the second heat exchanger to exchange LNG (Liquefied natural gas) with the high-pressure fluid or the first gas to convert the LNG into NG (natural gas) have.

The pretreatment separator may be a three phase separator that separates the first gas, the water, and the first liquid composed of a component having a specific gravity smaller than that of the water.

And a filtration unit installed between the crude oil storage tank and the first compressor to remove solid foreign substances and liquid foreign substances contained in the vapor.

According to the present invention, volatile organic compounds generated in a crude oil storage tank or the like can be treated by a series of continuous treatment processes to minimize atmospheric emissions. In addition, energy can be recovered in multiple stages in various ways during the treatment process, so that the energy efficiency of the volatile organic compound can be greatly improved by improving the energy efficiency and greatly increasing the operation efficiency of the ship, the equipment or other various devices .

1 is a configuration diagram of a volatile organic compound recovery apparatus according to a first embodiment of the present invention.
2 is a configuration diagram of a volatile organic compound recovery apparatus according to a second embodiment of the present invention.
3 is a configuration diagram of a volatile organic compound recovery apparatus according to a third embodiment of the present invention.
4 is a configuration diagram of a volatile organic compound recovery apparatus according to a fourth embodiment of the present invention.
5 is a configuration diagram of a volatile organic compound recovery apparatus according to a fifth embodiment of the present invention.
6 is a configuration diagram of a volatile organic compound recovery apparatus according to a sixth embodiment of the present invention.

BRIEF DESCRIPTION OF THE DRAWINGS The advantages and features of the present invention and methods for achieving them will become apparent with reference to the embodiments described in detail below with reference to the accompanying drawings. The present invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art. Is provided to fully convey the scope of the invention to those skilled in the art, and the present invention is only defined by the claims. Like reference numerals refer to like elements throughout the specification.

Hereinafter, the first to sixth embodiments of the present invention will be described in detail with reference to Figs. 1 to 6. Fig. A solid line arrow connecting the components in each of the figures attached to the specification together denote the 'flow' of the fluid and the 'channel' through which the fluid flows. Therefore, it can be understood that a pipeline is formed along the solid line arrows even if not marked with a separate code. In this specification, the 'second gas' and the 'second liquid' are defined as fluids generated by separating the gas-liquid separator into vapor and liquid.

First, referring to FIG. 1, a volatile organic compound recovery apparatus according to a first embodiment of the present invention will be described in detail.

1 is a configuration diagram of a volatile organic compound recovery apparatus according to a first embodiment of the present invention.

The volatile organic compound recovery device 1 of the present invention is a device for recovering volatile organic compounds from a crude oil storage tank (A), which is a continuous series of volatile organic compounds generated from crude oil (which may be filled with inert gas or the like, Through the processing step of FIG. The process steps include pressurizing, depressurizing, and regulating the temperature of the fluid through it, a phase change process and a process of separating fluids having different phases, and a process of controlling the temperature of fluids through different fluid-to-fluid heat exchanges. The apparatus 1 for recovering a volatile organic compound is composed of a plurality of components that are organically connected to each other to perform this process. The volatile organic compounds can be recovered through a series of processing steps by the operation of these components to minimize the emission amount and also to maximally recover the available energy of the volatile organic compounds, thereby greatly improving the energy efficiency.

Referring to FIG. 1, the apparatus 1 for recovering a volatile organic compound according to the first embodiment of the present invention is constructed as follows. The volatile organic compound recovery device 1 includes a first compressor 10 for compressing the vapor supplied from the crude oil storage tank A, a first heat exchanger 10 for cooling the high- Pressure fluid B passing through the first heat exchanger 20 or an expansion valve 30 for reducing the pressure of the first gas separated from the high-pressure fluid B through the pre-processing unit, an expansion valve 30, Or the second gas C1 is supplied to the combustion engine D by separating the first gas into the second gas C1 and the second liquid C2, (C2) supplies the gas-liquid separator (40) to the storage tank (100). The second gas C1 and the second liquid C2 can be produced in the gas-liquid separator 40 and supplied to the combustion engine D or stored in the storage tank 100 and used easily .

The volatile organic compound recovery apparatus 1 includes a preprocessing unit for separating the first gas from the high-pressure fluid B that has passed through the first compressor 10 and participating in the recovery process, . In the first embodiment of the present invention and the second embodiment described later, description will be made on the basis of the case where the preprocessing unit is not provided. In this case, the available energy is directly recovered from the high-pressure fluid (B) that has passed through the first compressor (10), and the first gas is not generated and is not involved in the energy recovery process. Hereinafter, with reference to FIG. 1, the components and the operation of the apparatus 1 for recovering a volatile organic compound according to the first embodiment of the present invention will be described in more detail.

The first compressor (10) compresses and pressurizes the vapor supplied from the crude oil storage tank (A). Crude oil is stored in the crude oil storage tank (A), and the vapor may include a volatile organic compound produced in crude oil and some other substance (such as an inert gas injected into the tank). The first compressor 10 pressurizes such vapor and converts it into a high-pressure fluid B. The first compressor 10 may be formed, for example, to increase the pressure of the fluid using a rotary vane rotating in a pressurizing chamber, or may be formed of a reciprocating compressor using a cylinder. However, it is not necessary to understand the manner in which the compressor is formed in this way as an example. Various types of compressors can be applied by selectively using a variety of various structures within a fluid compression range. The high-pressure fluid (B) compressed in the first compressor (10) is supplied to the first heat exchanger (20).

A filtration unit (90) is disposed at the front end of the first compressor (10). The filtration unit (90) is installed between the crude oil storage tank (A) and the first compressor (10) to remove solid foreign substances and liquid foreign substances contained in the vapor. Unnecessary foreign substances contained in the vapor can be removed by the filtration unit 90 and a more pure gas including volatile organic compounds can be supplied to the first compressor 10 to improve the compression ratio and the energy recovery capability. The filtration unit 90 may include a scrubber, a centrifugal separator, and the like. The filtration unit 90 may be used to remove foreign substances such as soot and liquid droplets from the vapor, ).

The crude oil storage tank (A) may be installed on a ship such as a crude oil carrier, but is not limited thereto. The crude oil storage tank (A) includes crude oil refining facilities, transportation facilities, storage facilities, and various other types of facilities capable of storing and retrieving crude oil. The crude oil storage tank (A) stores crude oil that generates volatile organic compounds, and the volatile organic compound recovery apparatus (1) of the present invention can effectively recover the volatile organic compounds generated in the crude oil and the available energy contained therein. Since the crude oil storage tank (A) is a facility for storing a substance that causes volatile organic compounds such as crude oil, even if not described separately, the volatile organic compound recovery apparatus 1 of the present invention is applied to the crude oil storage tank A ). That is, although the crude oil storage tank (A) is exemplified and described in the present specification, the present invention can be applied to various other facilities where volatile organic compounds are generated, so that the technical idea of the present invention is limited to storage facilities such as crude oil There is no need to interpret it.

The first heat exchanger (20) cools the high-pressure fluid (B) that has passed through the first compressor (10). The high-pressure fluid (B) that has passed through the first compressor (10) and whose temperature has been raised passes through the first heat exchanger (20) and is cooled. The first heat exchanger 20 may include at least one passage connected to be heat-exchangable, and may be formed in a structure in which a passage through which the high-pressure fluid B flows and a passage through which the cooling water flows are in contact with each other to enable heat exchange. The cooling water supplied to the first heat exchanger 20 may be clear water, distilled water, or the sea water may be used as cooling water when the present invention is applied to a facility such as a ship. Depending on the situation, the high-pressure fluid (B) can be cooled by exchanging heat with various kinds of cooling water.

The high-pressure fluid (B) that has passed through the first heat exchanger (20) passes through the expansion valve (30) and is reduced in pressure. That is, the high-pressure fluid (B) pressurized by the first compressor (10) is expanded by the expansion valve (30) to depressurize and rapidly lower the temperature. The temperature of the fluid can be lowered to a temperature at which it can be easily operated in the gas-liquid separator 40 at the subsequent stage. The expansion valve 30 may be, for example, a Joule-Thomson effect that reduces the pressure of the pressurized fluid passing through the nozzle. The depressurization rate of the expansion valve 30 can be appropriately set or adjusted in consideration of the operating temperature and the pressure of the gas-liquid separator 40.

The gas-liquid separator 40 separates the high-pressure fluid B (that is, the fluid that is compressed and reduced in pressure while passing through the expansion valve as described above with the fluid supplied to the expansion valve in the high-pressure state) through the expansion valve 30, (C1) and the second liquid (C2). The separated second gas C1 is supplied to the combustion engine D and the second liquid C2 is supplied to the storage tank 100. [ The second gas (C1) and the second liquid (C2) are collected by separating the vapor containing the above-mentioned volatile organic compounds into vapor and liquid and contain a combustible component, and are directly used as the fuel of the combustion engine It can be used as fuel after conversion to gaseous state. The gas-liquid separator 40 may be formed so as to separate the second base C1 and the second liquid C2 by density difference. The gas-liquid separator 40 discharges the second base C1 and the second liquid C2 In the form of a container or a drum.

As described above, the fluid supplied to the gas-liquid separator 40 after being decompressed and cooled by the expansion valve 30 can be separated into vapor and liquid and can be used directly as fuel or can be stored in a usable state as fuel. It can also be used to lower the temperature by heat exchange with the high-pressure fluid B before being used or stored as fuel (see the second to sixth embodiments described later). That is, the gas phase and the liquid phase components (the second gas and the second liquid) generated by the cooling process of the expansion valve 30 and the phase separation process of the gas-liquid separator 40 are provided as fuel so that the available energy is efficiently Is recovered. The second gas C1 is supplied to the combustion engine D and consumed after cooling the high pressure fluid B in the second heat exchanger 50 and the second liquid C2 is supplied to the second heat exchanger 50 The cooled high-pressure fluid B is re-cooled in the third heat exchanger 60 and stored in the storage tank 100. In this way, the fluid containing the volatile organic compound can be treated stepwise to recover the available energy and greatly reduce the emission amount.

The combustion engine D for introducing and consuming the second base C1 may include a gas turbine or a gas burner. When the combustion engine (D) is an engine that generates rotational power such as a gas turbine, it is possible to produce electric power by combining the generator with the rotary shaft of the gas turbine. The waste heat is recovered at the rear end of the gas turbine to generate steam, And a heat recovery steam generator (HRSG) that produces energy can be combined to greatly increase the energy recovery rate. The second liquid C2, which is stored in the storage tank 100, may be supplied to the gas turbine, or may be a gas turbine or a gas burner. Alternatively, the gas turbine may be selectively connected to drive a generator connected to the gas turbine, To the combustion engine D without passing through the heater 80. In this case, the gas in the storage tank 100 may be directly heated by the heater 80, So as to cope with the operating conditions and load fluctuations of the combustion engine D. By utilizing the recovered available energy in this way, energy efficiency can be greatly improved.

Hereinafter, a volatile organic compound recovery apparatus according to a second embodiment of the present invention will be described in detail with reference to FIG. For the sake of brevity and clarity, the description of components different from those of the above-described embodiments will be focused on, and the description of the components not mentioned separately will be replaced with the above description.

Referring to FIG. 2, the apparatus for recovering a volatile organic compound 1-1 according to the second embodiment of the present invention is configured as follows. The volatile organic compound recovery device 1-1 comprises a first compressor 10 for compressing the vapor supplied from the crude oil storage tank A and a second compressor 10 for cooling the high pressure fluid B which has passed through the first compressor 10, A heat exchanger 20, a high-pressure fluid B which has passed through the first heat exchanger 20 or an expansion valve 30 which decompresses a first gas separated from the high-pressure fluid B through a pre- The high pressure fluid B that has passed through the combustion chamber D or the first gas is divided into the second gas C1 and the second liquid C2 to supply the second gas C1 to the combustion engine D, 2 liquid C2 is supplied to the gas-liquid separator 40 which is supplied to the storage tank 100, the second gas C1 which is installed between the first heat exchanger 20 and the expansion valve 30 and is separated from the gas-liquid separator 40 A second heat exchanger 50 for exchanging heat with the high pressure fluid B or the first gas and a second heat exchanger 50 provided between the second heat exchanger 50 and the expansion valve 30, The second liquid C2, the high-pressure fluid B, 1 comprises a third heat exchanger 60 to heat the gas.

The apparatus for recovering a volatile organic compound 1-1 according to the second embodiment of the present invention includes a second heat exchanger 50 and a third heat exchanger 50 between the first heat exchanger 20 and the expansion valve 30, 60 is installed to cool the fluid step by step. The second heat exchanger 50 and the third heat exchanger 60 are connected to the expansion valve 30 by using the second base C1 and the second liquid C2 separated from the gas-liquid separator 40 as refrigerant, It is possible to greatly improve the cooling efficiency of the fluid. The remaining constitutions of the second heat exchanger 50 and the third heat exchanger 60 are substantially the same as those described above, so that the description thereof will be omitted, and the description of the second heat exchanger 50 and the third heat exchanger 60 and the operation and effect of the recovery device including the same will be described in detail.

The second heat exchanger 50 and the third heat exchanger 60 are installed on the flow path through which the high-pressure fluid B flows toward the expansion valve 30 as shown in the figure. The second heat exchanger 50 is installed between the first heat exchanger 20 and the expansion valve 30 and flows into the second base C1 separated from the gas-liquid separator 40 to perform heat exchange with the high- . The third heat exchanger 60 is installed between the second heat exchanger 50 and the expansion valve 30 and flows in the second liquid C2 separated from the gas-liquid separator 40, . The second heat exchanger (50) and the third heat exchanger (60) may also include a flow path connected to one or more heat exchangeable flow paths, and a flow path through which the high pressure fluid (B) 2 flow path through which the liquid C2 flows can be made to be heat-exchangeable.

As described above, the fluid supplied to the gas-liquid separator 40 after being decompressed and cooled by the expansion valve 30 can be separated into vapor and liquid and can be used directly as fuel or can be stored in a usable state as fuel. It can also be used to lower the temperature by heat exchange with the high-pressure fluid B before being used or stored as fuel. That is, the gas phase and the liquid phase components (the second gas and the second liquid) generated by the cooling process of the expansion valve 30 and the phase separation process of the gas-liquid separator 40 are supplied from the upstream side of the expansion valve 30 to the high- The cooling efficiency of the high-pressure fluid (B) is greatly improved, and is then supplied as fuel so that the available energy is effectively recovered through various paths. The second gas C1 is supplied to the combustion engine D and consumed after cooling the high pressure fluid B in the second heat exchanger 50 and the second liquid C2 is supplied to the second heat exchanger 50 The cooled high-pressure fluid B is re-cooled in the third heat exchanger 60 and stored in the storage tank 100. In this way, the fluid containing the volatile organic compound can be treated stepwise to recover the available energy and greatly reduce the emission amount.

Hereinafter, a volatile organic compound recovery apparatus according to a third embodiment of the present invention will be described in detail with reference to FIG. For the sake of brevity and clarity, the description of components different from those of the above-described embodiments will be focused on, and the description of the components not mentioned separately will be replaced with the above description.

3 is a configuration diagram of a volatile organic compound recovery apparatus according to a third embodiment of the present invention.

Referring to FIG. 3, the apparatus for recovering volatile organic compounds (1-2) according to the third embodiment of the present invention separates the first gas from the high-pressure fluid (B) that has passed through the first compressor (10) And a pre-processing unit (70) for engaging. In this case, the high-pressure fluid B having passed through the first compressor 10 is separated into the first base B1 and the first liquid B2 in the pre-processing unit 70. [ The first base B1 is collected into the second base C1 and the second liquid C2 through the process of pressure change, thermal change, phase change, etc., and the first liquid B2 is collected into the storage tank 100 . By providing the preprocessing unit 70, the fluid treatment capacity at the downstream can be reduced, the energy of each process can be reduced, and the available energy recovery can be increased. Hereinafter, with reference to FIG. 3, the constituent elements and actions of the apparatus for recovering a volatile organic compound (1-2) according to the third embodiment of the present invention will be described in more detail.

The pretreatment unit 70 is disposed between the first heat exchanger 20 and the second heat exchanger 50 as shown. The pretreatment unit 70 separates the high pressure fluid B having passed through the first heat exchanger 20 into the first base B1 and the first liquid B2 and the first base B1 into the second heat exchanger 50). The pretreatment unit 70 includes a pretreatment separator 71. The pretreatment separator 71 is installed between the first heat exchanger 20 and the second heat exchanger 50 to separate the high pressure fluid B from the first gas B1, and provides it to the second heat exchanger (50). The first base B1 separated in the pretreatment separator 71 is supplied to the expansion valve 30 through an additional treatment process and is then reduced in pressure through the expansion valve 30 so that the temperature is significantly lowered. The first gas B1 decompressed and cooled flows into the gas-liquid separator 40 and is separated into the second gas C1 and the second liquid C2 again and is discharged through the second heat exchanger 50 And a third heat exchanger 60 for heat exchange with the first base B1.

The first base B1 at the downstream end of the pretreatment unit 70 passes through the second heat exchanger 50, the third heat exchanger 60, the expansion valve 30 and the gas-liquid separator 40, The fluid B passes through the second heat exchanger 50, the third heat exchanger 60, the expansion valve 30, the gas-liquid separator 40, and the like. Therefore, a detailed description thereof is superseded by the above description. That is, the first base B1 supplied from the preprocessing unit 70 to the second heat exchanger 50 is cooled by heat exchange with the second base C1 provided in the second heat exchanger 50, (50) to the third heat exchanger (60), exchanges heat with the second liquid (C2) provided in the third heat exchanger (60), and is cooled again. The first base B1 thus cooled stepwise is reduced in pressure as it passes through the expansion valve 30 and is rapidly lowered in temperature and separated into the second base C1 and the second liquid C2 in the gas-liquid separator 40 . As described above, the second base C1 and the second liquid C2 are consumed in the combustion engine D after passing through the second heat exchanger 50 and the third heat exchanger 60, ) And used as needed.

That is, the volatile organic compound recovery apparatus 1-2 according to the third embodiment of the present invention separates the first base B1 from the high-pressure fluid B through the preprocessing unit 70, Participate. The first base B1 separates water and a liquid component from the high-pressure fluid B by using the pretreatment separator 71. The first base B1 serves as a vapor phase component in the post- The energy consumed in the process can be reduced. The pretreatment unit 70 includes a second compressor 73 for further pressurizing the first base B1 at the rear end of the pretreatment separator 71 to compress the first base B1 to a higher pressure, The first gas B 1 can be cooled to a sufficiently low temperature and supplied to the gas-liquid separator 40 by maximizing the decompression effect of the first gas B 1. Accordingly, the cooling efficiency of the second heat exchanger (50) and the third heat exchanger (60) can be improved. Hereinafter, the configuration of the preprocessing unit 70 will be described in more detail.

The pretreatment unit 70 includes the pretreatment separator 71, the moisture removal unit 72, the second compressor 73, and the fourth heat exchanger 74 described above. The pretreatment separator 71 is installed between the first heat exchanger 20 and the second heat exchanger 50 to introduce the high pressure fluid B having passed through the first heat exchanger 20, The gas B1, the water B3, and the first liquid B2. The pretreatment separator 71 separates the high-pressure fluid B into a first liquid B2 as a gaseous component, water B3 and a first liquid B2 having a specific gravity smaller than that of the water B3 Phase separator. The separated first base B1 passes through the water elimination unit 72, the second compressor 73 and the fourth heat exchanger 74 to be processed to the second heat exchanger 50 side / RTI > The first liquid B2 is stored in the storage tank 100 as shown and used together with the second liquid C2 as required. The first liquid B2 and the second liquid C2 may be stored together in the storage tank 100 or may be stored separately. The water B3 may be stored in a wastewater storage tank, for example, a slop tank such as a crude oil carrier.

The water removal unit 72 is installed between the pretreatment separator 71 and the second heat exchanger 50 to remove moisture from the first base B1. Thus, the first base body B1 is converted to a more pure gas phase component and is further converted into a state of easy compression. The second compressor 73 is disposed between the pretreatment separator 71 and the second heat exchanger 50 and disposed at the rear end of the water removal unit 72. The first base B1, through which moisture has been removed through the water removal unit 72, passes through the second compressor 73 and is compressed to a higher pressure. That is, the high-pressure fluid B is generated by passing through the first compressor 10 described above and passed through the pretreatment separator 71 to separate the gaseous component (the first gas) The first base B1 of the high pressure state can be supplied to the expansion valve 30 by pressurizing the first valve B1 to the second compressor 73 again. The second compressor 73 may also be formed, for example, to increase fluid pressure using a rotating blades in a pressurizing chamber, or may be formed of a reciprocating compressor using a cylinder. However, it is not necessary to understand the formation method of the compressor as an example of this, and various types of compressors can be applied by selectively using a variety of various structures as far as the compression of the fluid is possible. The second compressor (73) compresses the first base (B1) from which the liquid component is separated from the high-pressure fluid (B), so that the second compressor (73) can be installed with a small amount of driving energy and a relatively small capacity.

The first base B1 passing through the second compressor 73 passes through the fourth heat exchanger 74 and is preferentially cooled. The fourth heat exchanger 74 is installed between the second compressor 73 and the second heat exchanger 50 and is disposed between the second heat exchanger 50 and the third heat exchanger 60 ) Is formed. Whereby the temperature of the first base body (B1) compressed at a high pressure can be easily cooled to a more appropriate temperature. The fourth heat exchanger 74 may include a flow path structure connected to allow heat exchange and may be formed in a structure in which the flow path through which the first base B1 flows and the flow path through which the cooling water flows are in contact with each other to enable heat exchange . As the cooling water, clear water, distilled water and the like can be used. In the case where the present invention is applied to a facility such as a ship, sea water can be used as cooling water. Various kinds of cooling water may be provided to the fourth heat exchanger 74 to cool the first base B1 according to the circumstances.

The first base body B1 in a high pressure state is provided to the second heat exchanger 50 side from the pretreatment unit 70 constructed as described above. The first base B1 is cooled and depressurized through the above-described process, is rapidly depressurized in a high-pressure state, and is supplied to the gas-liquid separator 40 at a sufficiently low temperature. The second base C1 and the second liquid C2 can be generated through the second heat exchanger 50 and the second liquid C2 as described above, After passing through the third heat exchanger 60, may be supplied to the combustion engine D or stored in the storage tank 100 and used as needed. Also, the first liquid B2 may be stored in the storage tank 100 together with the second liquid C2 or may be separately stored and used as needed. As described above, it is possible to more efficiently recover the available energy of the volatile organic compounds, thereby increasing the energy efficiency and minimizing the emission of volatile organic compounds.

Hereinafter, a volatile organic compound recovery apparatus according to a fourth embodiment of the present invention will be described in detail with reference to FIG. For the sake of brevity and clarity, the description of components different from those of the above-described embodiments will be focused on, and the description of the components not mentioned separately will be replaced with the above description.

4 is a configuration diagram of a volatile organic compound recovery apparatus according to a fourth embodiment of the present invention.

4, the apparatus for recovering volatile organic compounds 1-3 according to the fourth embodiment of the present invention is a system in which a first base body B1 between a second compressor 73 and a gas-liquid separator 40 flows, And a high-pressure tank 110 connected to the branch pipe 111 and branch pipe 111 branched from the high-pressure pipe 110 and storing the first base B1. The high pressure tank 110 may be configured to introduce and store the first base B1 compressed in a multi-stage pressure state via the branch pipe 111 and to discharge and use the first base B1 when necessary. The branch pipe 111 may be provided with a regulating valve 120 to regulate the pressure of the first base B1 flowing into the high pressure tank 110. The branch pipe 111 may be branched from a pipe connecting the fourth heat exchanger 74 and the second heat exchanger 50 as shown in the figure.

The first base B1 stored in the high-pressure tank 110 can be provided, for example, in a combustion engine D. [ Although not shown, a supply pipe (not shown) for connecting between the high-pressure tank 110 and the combustion engine D is formed and a valve capable of reducing the pressure is added to the front end of the combustion engine D of the supply pipe, B1) to the combustion engine (D). Particularly, when the combustion engine D is formed by a gas turbine or the like, the first base B1 stored in the high-pressure tank 110 is quickly supplied to the combustion engine D can do. (Not shown) for discharging the liquid component to the storage tank 100 when the first base B1 in the high-pressure tank 110 is condensed to generate liquid components. In this way, the available energy can be recovered through the structure including the high-pressure tank 110 and utilized more effectively.

Hereinafter, a VOC recovery apparatus according to a fifth embodiment of the present invention will be described in detail with reference to FIG. For the sake of brevity and clarity, the description of components different from those of the above-described embodiments will be focused on, and the description of the components not mentioned separately will be replaced with the above description.

5 is a configuration diagram of a volatile organic compound recovery apparatus according to a fifth embodiment of the present invention.

5, the apparatus for recovering a volatile organic compound 1-4 according to the fifth embodiment of the present invention is installed between a first heat exchanger 20 and a second heat exchanger 50, and is provided with a Liquefied Natural Gas And an evaporator 130 for exchanging heat between the high-pressure fluid B and the first base B1 to convert the LNG into NG (natural gas). The evaporator 130 may include a flow path structure interconnected to enable heat exchange. The evaporator 130 may include a first flow path through the first flow path B1 and a second flow path from the first flow path, (B1). ≪ / RTI > The cryogenic LNG E1 is heat exchanged with the first base B1 to be vaporized and converted to NG (E2) and supplied to the consumer F. Although the construction of the evaporator 130 for converting the LNG E1 into the NG (E2) by heat exchange with the first base B1 is shown in the figure, if the pre-treatment unit 70 is not provided, the first heat exchanger 20 Pressure fluid B to the evaporator 130 and heat exchange with the LNG E1 to convert it to NG (E2) by connecting a pipeline between the evaporator 130 and the evaporator 130. [

That is, when the volatile organic compound recovery device 1-4 is applied to a ship or a facility using the LNG storage tank E or the like to vaporize the LNG E1 and use it as a fuel, the LNG (E1) So that the cooling efficiency can be greatly increased. At the same time, it is not necessary to additionally provide a vaporizer for vaporizing the LNG (E1) in the consumption site (F), which is also effective in terms of device configuration. The LNG E1 may be supplied to the evaporator 130 by a pump 140 or the like connected between the evaporator 130 and the LNG storage tank E and the NG E2 vaporized by the evaporator 130 may be supplied to the consumer F ). ≪ / RTI > The consuming place F includes an internal combustion engine using NG (E2) as fuel, a boiler, a turbine, and the like, and it is possible to control the pump 140 and adjust the NG (E2) supply amount in accordance with the load fluctuation. The volatile organic compound recovery apparatus 1-4 can be easily applied to a facility provided with the LNG storage tank E or the like.

Hereinafter, a VOC recovery apparatus according to a sixth embodiment of the present invention will be described in detail with reference to FIG. For the sake of brevity and clarity, the description of components different from those of the above-described embodiments will be focused on, and the description of the components not mentioned separately will be replaced with the above description.

6 is a configuration diagram of a volatile organic compound recovery apparatus according to a sixth embodiment of the present invention.

Referring to FIG. 6, in the volatile organic compound recovery apparatus 1-5 according to the sixth embodiment of the present invention, the water removal unit 72 is disposed at the front end of the pretreatment separator 71. A water removal unit 72 is disposed between the first heat exchanger 20 and the pretreatment separator 71 to remove moisture contained in the high pressure fluid B flowing into the pretreatment separator 71 from the pretreatment separator 71, It is possible to pre-process it before it is introduced. Therefore, it is not necessary to form the pretreatment separator 71 as a three-phase separator as described above, and the pretreatment can be performed by the gas-liquid separator for separating the high-pressure fluid B into the first base B1 and the first liquid B2, The separator 71 can be constituted. This minimizes the generation of unnecessary adducts and makes it possible to efficiently configure the apparatus, and it is possible to more efficiently recover the available energy of the volatile organic compounds and to minimize the amount of emission through the process as described above.

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it is clearly understood that the same is by way of illustration and example only and is not to be taken in conjunction with the present invention. You will understand. It is therefore to be understood that the above-described embodiments are illustrative in all aspects and not restrictive.

1, 1-1, 1-2, 1-3: volatile organic compound recovery device
10: first compressor 20: first heat exchanger
30: expansion valve 40: gas-liquid separator
50: second heat exchanger 60: third heat exchanger
70: preprocessing unit 71: preprocessing separator
72: water removal unit 73: second compressor
74: fourth heat exchanger 80: heater
90: Filtration unit 100: Storage tank
110: high pressure tank 111: branch pipe
120: regulating valve 130: evaporator
140: Pump A: Crude oil storage tank
B: high-pressure fluid B1: first gas
B2: first liquid B3: water
C1: Secondary gas C2: Second liquid
D: Combustion engine E: LNG storage tank
E1: LNG E2: NG
F: Consumer

Claims (12)

A first compressor for compressing the vapor supplied from the crude oil storage tank;
A first heat exchanger for cooling the high-pressure fluid passing through the first compressor;
An expansion valve for decompressing the high pressure fluid that has passed through the first heat exchanger or the first gas separated from the high pressure fluid that has passed through the first heat exchanger through the preprocessing unit;
The high pressure fluid passing through the expansion valve or the first gas passing through the expansion valve is separated into a second gas and a second liquid so that the second gas is supplied to the combustion engine, Liquid separator; And
Liquid separator provided between the first heat exchanger and the expansion valve and the high-pressure fluid passed through the first heat exchanger or the high-pressure fluid passed through the first heat exchanger, And a second heat exchanger for exchanging heat with the first gas. delete 2. The gas-liquid separator according to claim 1, further comprising: a second liquid that is provided between the second heat exchanger and the expansion valve and is separated from the gas-liquid separator; and the second liquid that has passed through the second heat exchanger, And a third heat exchanger for exchanging heat with the first gas. The image processing apparatus according to claim 3,
Further comprising a pretreatment separator provided between the first heat exchanger and the second heat exchanger for separating the first gas from the high pressure fluid passed through the first heat exchanger and providing the first gas to the second heat exchanger, Device. The image processing apparatus according to claim 4,
Further comprising a moisture removing unit provided between the first heat exchanger and the pre-treatment separator, or between the pre-treatment separator and the second heat exchanger. The image processing apparatus according to claim 4,
And a second compressor installed between the pre-treatment separator and the second heat exchanger to press the first gas separated from the high-pressure fluid passed through the first heat exchanger. The apparatus of claim 6, further comprising a fourth heat exchanger installed between the second compressor and the second heat exchanger to cool the first gas passed through the second compressor. The gas turbine according to claim 6, further comprising: a branch pipe branched from a pipeline through which the first gas flows between the second compressor and the gas-liquid separator; and a second gas pipe connected to the branch pipe, And a high-pressure tank for supplying the volatile organic compound. The volatile organic compound recovery apparatus according to claim 8, further comprising a regulating valve formed in the branch pipe and regulating the pressure of the first gas introduced into the high-pressure tank. [4] The apparatus as claimed in claim 3, further comprising: an LNG (Liquefied Natural Gas) disposed between the first heat exchanger and the second heat exchanger, and a high pressure fluid having passed through the first heat exchanger or the high pressure fluid passing through the first heat exchanger And an evaporator for converting the LNG into a natural gas (NG) by heat-exchanging the separated first gas. 5. The volatile organic compound recovery apparatus according to claim 4, wherein the pretreatment separator is a three-phase separator for separating the first gas, the water, and the first liquid composed of a component having a specific gravity smaller than that of the water. The volatile organic compound recovery apparatus according to claim 1, further comprising a filtration unit installed between the crude oil storage tank and the first compressor to remove solid foreign substances and liquid foreign substances contained in the vapor.

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