KR20130076123A - Pure oxygen combustion type submerged vaporizer - Google Patents

Abstract

PURPOSE: A pure oxygen combustion type vaporizing apparatus is provided to reduce the amount of carbon dioxide which is discharged from a liquefied natural gas (LNG) vaporizing unit by improving combustion efficiency of a burner. CONSTITUTION: A pure oxygen combustion type vaporizing apparatus (1) comprises a liquefied natural gas (LNG) storage unit (100), an LNG vaporizing unit (200), an oxygen production unit (300), a carbon dioxide liquefying unit (400), and a liquefied carbon dioxide storage unit (500). The LNG vaporizing unit comprises a water tank (210); a burner (220) which is provided inside the water tank, and heats the water in the water tank by burning a fuel gas; and a first heat exchanger (230) which is provided inside the water tank, and which vaporizes the LNG that is supplied from the LNG storage unit, passes through the first heat exchanger, and exchanges heat with the water heated inside the water tank. The oxygen production unit produces oxygen, and supplies oxygen to the burner. The carbon dioxide liquefying unit gathers carbon dioxide from exhaust gas which is discharged from the LNG vaporizing unit, and liquefies the gathered carbon dioxide. The liquefied carbon dioxide storage unit stores the carbon dioxide which is liquefied by the carbon dioxide liquefying unit.

Description

Pure oxygen combustion type Submerged Vaporizer

The present invention relates to a pure oxygen combustion vaporizer, and more particularly, to a pure oxygen combustion vaporizer that can be burned by supplying high purity oxygen instead of air in a burner and collecting and storing carbon dioxide in the generated exhaust gas. will be.

In general, liquefied natural gas, that is, LNG (Liquefied Natural Gas) refers to a colorless, odorless and transparent ultra low temperature (-162 ℃) liquefied gas that is cooled from the source to reduce the volume to 1/600 for the transport and storage of natural gas.

LNG is transported from the mountain to the LNG takeover base by LNG carriers and stored in specially manufactured LNG storage tanks. The stored LNG is vaporized in an LNG vaporizer for supply and supplied to demand.

LNG has a total of 200Kcal of cold heat energy per kilogram and undergoes a vaporization process to supply gas to customers.

In the vaporization process, a Submerged Combustion Vaporizer (SMV) is also used. The combustion vaporizer vaporizes LNG at -160 ° C into natural gas at 0 ° C by using heat generated by combustion of fuel gas. .

Conventional combustion vaporizer is, for example, the combustion vaporizer disclosed in the accompanying drawing 2 of the registered patent of Korea Patent Registration No. 10-1000510, and includes a water tank, a heat exchanger and a burner installed in the water tank as disclosed .

The burner is supplied with fuel gas and air, and the water in the tank is heated up by the heat generated during combustion of the fuel gas. And the bubbles generated in the tank rises to convection the water. At this time, the LNG passing through the heat exchanger, specifically the LNG tube, is vaporized while being heated with the heated water in the tank.

Such a combustion vaporizer generates a large amount of carbon dioxide upon combustion of fuel gas, and the generated carbon dioxide is discharged into the air through an exhaust pipe.

On the other hand, Korea is one of the most prominent countries for the second mandatory reduction of greenhouse gases along with Brazil, China and India during the second commitment of the Kyoto Protocol, which will begin in 2012.

Therefore, in order to actively cope with such a change, a method of recovering and treating carbon dioxide emitted from the above-described conventional combustion vaporizer should be sought.

The present invention has been made to solve the problems of the conventional combustion carburetor described above, in order to effectively capture and store the carbon dioxide discharged from the combustion carburetor, a pure oxygen combustion vaporizer that burns using pure oxygen instead of air combustion. I would like to present.

In addition, the present invention is to provide a pure oxygen combustion vaporizer to prevent carbon dioxide is discharged into the air by collecting and storing carbon dioxide in the exhaust gas generated in the combustion vaporizer.

In order to solve the above problems, the oxy-fuel type vaporization apparatus according to the present invention, LNG storage means for storing LNG (Liquefied Natural Gas); A water tank, a burner provided in the water tank and the fuel gas is combusted so that the water in the water tank is heated, and the LNG provided in the water tank and supplied from the LNG storage means passes and exchanges heat with the heated water in the water tank. LNG vaporization means comprising a first heat exchanger to be vaporized; Oxygen production means for producing oxygen and supplying oxygen to the burner; Carbon dioxide liquefaction means for collecting and liquefying carbon dioxide from the exhaust gas discharged from the LNG vaporization means; And liquefied carbon dioxide storage means for storing carbon dioxide liquefied by the carbon dioxide liquefaction means.

In this case, the fuel gas may be NG (Natural Gas) vaporized by the LNG vaporization means.

And, the oxygen production means, the air filter for filtering the air introduced from the outside; An air compressor for compressing air passing through the air filter; An adsorption tower into which air compressed by the air compressor is introduced, and zeolite is filled therein so that nitrogen is adsorbed and oxygen is permeated and discharged from the introduced air; And oxygen storage means connected to the burner to store oxygen discharged from the adsorption tower and to supply oxygen to the burner.

In addition, the oxygen production means, an air cooler to cool the air compressed in the air compressor; And a water separator connected to the adsorption tower such that water in the air cooled by the air cooler is separated, so that gaseous air is supplied to the adsorption tower.

The oxygen storage means may include a buffer tank storing oxygen discharged from the adsorption tower; And an oxygen holder for receiving oxygen from the buffer tank and storing the oxygen and supplying the oxygen to the burner.

At this time, the oxygen supply amount adjusting means for adjusting the flow rate of the oxygen supplied from the oxygen holder to the burner; may be further included.

The oxygen supply amount adjusting means, the solenoid valve for adjusting the flow rate of oxygen supplied from the oxygen holder to the burner; An oxygen sensor for measuring the amount of oxygen in the exhaust gas discharged from the LNG vaporization means; And a control unit which receives the detection signal of the oxygen sensor and controls the operation of the solenoid valve.

The oxygen production means may be connected to the adsorption tower, and a vacuum pump may be configured to decompress the inside of the adsorption tower to separate nitrogen adsorbed from the adsorption tower and to be discharged from the adsorption tower.

At this time, the oxygen production means, is connected to the vacuum pump so that the nitrogen discharged through the vacuum pump from the adsorption tower to the outside, a silencer to remove the noise generated by the vacuum pump may further include; .

On the other hand, the carbon dioxide liquefaction means, an exhaust gas compressor that is generated after the combustion of the fuel gas and discharged from the LNG vaporization means is compressed; An exhaust gas cooler configured to cool the exhaust gas compressed by the exhaust gas compressor; A molecular filter (Molecular Sieve (MS)) which allows the remaining carbon dioxide to be discharged after the water molecules are separated from the exhaust gas cooled by the exhaust gas cooler; And heat exchange means for allowing the carbon dioxide discharged from the molecular filter to be liquefied while being heat exchanged and then discharged to the liquefied carbon dioxide storage means.

At this time, the heat exchange means, the condenser through which the heat exchange medium supplied from the outside passes; And a second heat exchanger configured to pass through the heat exchange medium discharged from the condenser, and to exchange heat with the heat exchange medium while passing carbon dioxide discharged from the molecular filter. The liquid may be liquefied as it is exchanged with the heat exchange medium supplied to the condenser and supplied to the condenser from the outside.

The carbon dioxide liquefaction means is connected to the second heat exchanger to pass through the heat exchange medium discharged from the second heat exchanger, and is connected to the exhaust gas compressor and the exhaust gas cooler and discharged from the exhaust gas compressor. And a third heat exchanger configured to supply heat to the exhaust gas cooler after the exhaust gas passes through the heat exchange medium.

On the other hand, the heat exchange medium supplied to the condenser may be made of LNG discharged from the LNG storage means.

According to the present invention, since the oxygen produced by the oxygen production means is supplied to the burner and combusted, the oxygen is burned in the burner, so that the combustion efficiency in the burner is improved, whereby the carbon dioxide discharged from the LNG vaporization means is The amount can be reduced.

In addition, by including the carbon dioxide liquefaction means and the liquefied carbon dioxide storage means, it is possible to easily collect and store carbon dioxide from the exhaust gas discharged by the pure oxygen combustion, so that carbon dioxide is not discharged to the outside air.

1 is a schematic diagram of a pure oxygen combustion vaporization apparatus according to a preferred embodiment of the present invention,
2 is a system diagram of the oxygen production means shown in FIG.
3 is a system diagram of the carbon dioxide liquefaction means and liquefied carbon dioxide storage means shown in FIG.
FIG. 4 is a system diagram of a combustion vaporization apparatus further including an oxygen supply amount adjusting means in the combustion vaporization apparatus illustrated in FIG. 1.

With reference to the accompanying drawings, a pure oxygen combustion vaporization apparatus according to a preferred embodiment of the present invention will be described in detail.

As shown in FIG. 1, the pure oxygen combustion vaporization apparatus 1 according to an exemplary embodiment of the present invention may include an LNG storage means 100, an LNG vaporization means 200, an oxygen production means 300, and carbon dioxide liquefaction. Means 400 and liquefied carbon dioxide storage means 500 is included.

The LNG storage means 100 may be configured as a storage tank in which LNG (Liquefied Natural Gas) is stored, and the LNG stored therein may be LNG having a very low temperature, for example, a temperature of −155 ° C. And LNG storage means 100 may be composed of one storage tank or more storage tanks.

LNG vaporization means 200, a conventional Submerged Combustion Vaporizer (SMV) may be presented as an example.

In this case, the LNG vaporization means 200 may include a water tank 210, a burner 220, and a first heat exchanger 230.

The water tank 210 is stored in the water, the burner 220 is provided in the water tank 210. The burner 220 receives air and fuel gas from the outside, and heats the water in the water tank 210 by the heat generated while the fuel gas is burned.

The first heat exchanger 230 is provided inside the water tank 210 similarly to the burner 220. The first heat exchanger 230 is passed through the LNG supplied from the LNG storage means 100, so that the LNG can be supplied to the first heat exchanger 230 from the LNG storage means 100 and passed through, as shown in FIG. As described above, at least one pump 110 may be connected to the LNG storage means 100.

In the course of passing through the first heat exchanger 230, the LNG exchanges heat with water in the water tank 210 heated by the burner 220. And it is vaporized in the heat exchange process, and becomes NG (Natural Gas).

The vaporized NG is discharged from the LNG vaporization means 200 is supplied to the required demand destination, at this time, a part may be supplied to the burner 220 to be used as fuel gas of the burner 220.

On the other hand, the oxygen production means 300 is a means for producing high-purity oxygen (hereinafter referred to as "oxygen") to the burner 220.

The pure oxygen combustion vaporization apparatus 1 according to the present embodiment is configured such that the burner 220 included in the LNG vaporization means 200 does not simply receive air and burns, but receives pure oxygen.

Unlike air combustion, oxy-fuel combustion has no nitrogen in the object of combustion, so waste heat consumption is reduced and combustion efficiency is increased, resulting in reduced CO2 emissions. In addition, since the exhaust gas generated after the combustion in the burner 220 is mostly composed of carbon dioxide (CO₂) and water (H₂O), compared to when air is burned, the recovery and recovery of carbon dioxide is easy.

Oxygen production means 300, specifically, as shown in FIG. 2 may include an air filter 310, air compressor 320, adsorption tower 350, and oxygen storage means 360.

The air filter 310 is a means for filtering air introduced from the outside.

The air filtered by the air filter 310 is compressed (pressurized) by the air compressor 320 so that air is introduced into the adsorption tower 350 to be described later, and flows into the oxygen storage means 360 to be described later. )do. At this time, when pressurization to the air needs to be weighted, as shown, the return path 321 is opened and closed by the valve 322, and the path before the air compressor 320 along the return path 321 Repeated pressurization by the air compressor 320 may be performed on the air re-introduced into the furnace.

The air compressed by the air compressor 320 may be cooled in order to increase the adsorption force of nitrogen in the adsorption tower 350 to be described later. To this end, the oxygen producing means 300 according to the present embodiment may further include an air cooler 330 as shown.

Some of the air cooled by the air cooler 330 may be changed into water in accordance with the cooling, the adsorption tower 350 to be described later, since the introduction of air in the gaseous state helps to improve the nitrogen adsorption power, the present embodiment Oxygen production means 300 according to the example may further include a water separator (340) for separating such water.

The gaseous air in which water is separated while passing through the water separator 340 is introduced into the adsorption tower 350.

The adsorption tower 350 is a means for separating nitrogen from the air introduced into the inside, and is filled with zeolite (Zeolite) inside.

Zeolite shows strong adsorption performance with respect to nitrogen in air, and has weak adsorption performance with respect to oxygen. Accordingly, when air is supplied to the zeolite, nitrogen is adsorbed and oxygen is permeated and discharged to produce oxygen without nitrogen.

The adsorption tower 350 is filled with such zeolite, and may be composed of two or more zeolite packed towers connected horizontally and parallel as shown to increase the purity of oxygen and to enable continuous production of oxygen. have. However, these examples are not necessarily limited, and any general zeolite packed column used in the art may be used by adopting an appropriate one in structure or number. Hereinafter will be described based on the example of the adsorption tower 350 shown.

The gaseous air passing through the water separator 340 is introduced into one of the two adsorption towers 350 of the two adsorption towers 350, and the nitrogen molecules in the introduced air are before the oxygen molecules according to the difference in adsorption force. Adsorbed at

Nitrogen molecules are adsorbed until one of the adsorption towers 350 is saturated, and in this process, oxygen is permeated and discharged, that is, oxygen is produced and discharged.

When one of the adsorption tower 350 is saturated with the adsorbed nitrogen molecules, by operating the solenoid valve 351 by a control device (not shown), the air in the gaseous state through the water separator 340 is the other The adsorption tower 350 may be introduced into.

The other adsorption tower 350 is also produced and discharged through the same process as any of the adsorption tower 350 described above.

At this time, any one of the adsorption tower 350 saturated with the adsorbed nitrogen molecules may undergo a process of desorbing nitrogen for the reproduction of oxygen.

More specifically, the oxygen production means 300 according to the present embodiment may further include a vacuum pump 370 to separate nitrogen from the adsorption tower 350.

The vacuum pump 370 sucks air in the adsorption tower 350 to decompress the pressure in the adsorption tower 350 to an atmospheric pressure or a vacuum state so that the nitrogen adsorbed in the adsorption tower 350 is separated and separated. Nitrogen is induced to be discharged to the outside of the adsorption tower (350).

Nitrogen discharged to the outside of the adsorption tower 350 is not harmful even if discharged to the outside air can be immediately discharged to the outside air. However, considering that large noise is generated due to the air pressure generated by the vacuum pump 370, it is necessary to remove the noise prior to the discharge of nitrogen.

Therefore, the oxygen producing means 300 according to the present embodiment, so that the nitrogen discharged from the adsorption tower 350 through the vacuum pump 370, after the noise is removed before being discharged to the outside is discharged to the outside , May further include a silencer 380 connected to the vacuum pump 370.

The oxygen production means 300 includes two adsorption towers 350 connected in parallel, as shown, so that one of the adsorption towers 350 produces nitrogen while the other adsorption tower 350 produces oxygen. The separation and removal process, and during the production of oxygen in one of the other adsorption tower 350 to undergo a process of separating and removing nitrogen in one of the adsorption tower 350, the continuous oxygen in this iterative process Can be produced.

The pure oxygen produced by the oxygen production means 300 is moved to the oxygen storage means 360 and stored, and is supplied to the burner 220 as necessary.

As an example, the oxygen storage unit 360 may include a buffer tank 361 and an oxygen holder 362.

The oxygen discharged through the adsorption tower 350 is in a compressed state, and according to the load of the air compressor 320, the pressure of the discharged oxygen may vary, so that the oxygen may be discharged for stable output (discharge) of oxygen. A buffer tank 361 that can absorb and store pressure can be used.

Accordingly, oxygen discharged through the adsorption tower 350 may be stored in the first buffer tank 361, and oxygen stored in the buffer tank 361 may be introduced into an oxygen holder 362, which is a storage container of oxygen, to provide an oxygen holder ( 362).

Oxygen stored in the oxygen holder 362 is supplied to the burner 220 for combustion of the fuel gas in the burner 220 as described above. And, the excessively produced oxygen may be introduced into the muffler 380 as shown, so that it can be discharged into the outside air as needed.

In the illustrated example, an example in which two oxygen producing means 300 are provided in consideration of the oxygen production amount is provided, but is not limited thereto. Of course, it can be provided with 300).

On the other hand, the carbon dioxide liquefaction means 400 is a means for collecting and liquefying carbon dioxide from the exhaust gas discharged from the LNG vaporization means 200, that is, the exhaust gas generated and discharged by the burner 220.

Specifically, as illustrated in FIG. 3, the carbon dioxide liquefaction means 400 may include an exhaust gas compressor 421, 422, 423, an exhaust gas cooler 431, 432, 433, a molecular filter 440, and a heat exchange means.

As described above, since the exhaust gas discharged from the LNG vaporization means 200 is generated by combustion of pure oxygen and NG, most of the exhaust gas is composed of carbon dioxide (CO 2) and moisture (H 2 O).

The water may be separated from the water separator 410 to be drained, and the exhaust gas from which the water is removed is introduced into the exhaust gas compressor 421 and compressed, and subsequently the exhaust gas cooler ( 431 is cooled as it is introduced.

Since the triple point is formed at about 56.4 degrees Celsius and 5.18 bar, the carbon dioxide can be liquefied when the exhaust gas is compressed and cooled to a pressure above the triple point described above. Therefore, the exhaust gas compressors 421, 422, 423 and the exhaust gas coolers 431, 432, 433 are used for the liquefaction of carbon dioxide.

Shown is an example in which three exhaust gas compressors 421, 422, 423 and three exhaust gas coolers 431, 432, 433 are used for compression and cooling efficiency, but this is only one example, and the proper compression and cooling according to the given conditions is shown. An appropriate number of exhaust compressors and exhaust coolers may be included to achieve this.

Meanwhile, the carbon dioxide liquefaction means 400 according to the present embodiment may liquefy carbon dioxide using only the exhaust gas compressors 421, 422, 423 and the exhaust gas coolers 431, 432, 433, but considering the efficiency in the carbon dioxide liquefaction process, From the carbon dioxide and the LNG storage means 100 of the exhaust gas and the state before the liquefaction so that the process of vaporizing the LNG stored in the LNG storage means 100 may be accompanied by using the heat of the exhaust gas in the liquefaction process. The heat exchange is performed between the discharged LNG, which will be described in more detail below.

The exhaust gas may generate moisture (H 2 O) in the process of being compressed and cooled through the exhaust gas compressors 421, 422, 423 and the exhaust gas coolers 431, 432, 433. Therefore, a molecular filter (M / S tower) 440 may be included to remove the moisture.

The molecular filter 440 is a means for finally separating the remaining water from the exhaust gas so that only carbon dioxide is permeated and discharged, and various known fillers such as zeolite or alumina to prevent the water, ie, water molecules, from being permeated and discharged. Fillers such as may be filled therein.

The carbon dioxide from which water is removed through the molecular filter 440 is introduced into the heat exchange means.

Specifically, the heat exchange means may include a second heat exchanger 450 and a condenser 460.

First, the condenser 460 will be described. The condenser 460 is configured to finally liquefy carbon dioxide flowing into the condenser 460 while exchanging heat with a heat exchange medium.

Specifically, low temperature LNG flows into the condenser 460. In this case, the LNG may allow the LNG stored in the aforementioned LNG storage means 100 to be introduced. The process of allowing LNG stored in the LNG storage means 100 to be vaporized through a heat exchange process may be accompanied in the carbon dioxide liquefaction process.

The low temperature LNG discharged from the LNG storage means 100 and introduced into the condenser 460 becomes a heat exchange medium for cooling and liquefying carbon dioxide introduced into the condenser 460 through the second heat exchanger 450 to be described later. . Carbon dioxide is finally liquefied through this heat exchange in the condenser 460, and the liquefied carbon dioxide is moved to and stored in a carbon dioxide storage tank provided with at least one liquefied carbon dioxide storage unit 500 connected to the condenser 460, for example. do.

LNG introduced into the condenser 460 is discharged from the condenser 460 and flows into the second heat exchanger 450. At this time, the air staying in the inner space of the condenser 460 needs to be discharged together during the inflow and discharge of LNG. Since the air is also cooled by heat exchange with LNG, the air discharged from the condenser 460 is also second. It may be to be introduced into the heat exchanger 450.

The air introduced into the second heat exchanger 450 may be discharged to the outside through a vent after undergoing heat exchange in the second heat exchanger 450.

As described above, the low temperature LNG and the cooled air are introduced into the second heat exchanger 450 together. Carbon dioxide discharged from the above-described molecular filter 440 is also introduced into the second heat exchanger 450.

The carbon dioxide discharged from the molecular filter 440 is cooled while undergoing heat exchange with LNG and cooled air while passing through the second heat exchanger 450. The carbon dioxide thus cooled is liquefied by entering the condenser 460 as described above, and LNG is also changed into NG vaporized through heat exchange.

Meanwhile, the carbon dioxide liquefaction means 400 according to the present embodiment may further include a third heat exchanger 470 so as to improve the liquefaction efficiency of carbon dioxide and the vaporization efficiency of LNG.

As illustrated, the third heat exchanger 470 may be provided to be disposed between the exhaust gas compressor 423 and the exhaust gas cooler 433. As shown in the drawing, an example in which the third heat exchanger 470 is disposed between the third exhaust gas compressor 423 and the third exhaust gas cooler 433 is provided, but the present invention is not limited thereto. Of course, it may be disposed between the compressor (421,422) and the exhaust gas cooler (431,432).

When the third heat exchanger 470 is further included, the compressed exhaust gas is introduced into the third heat exchanger 470 through the third exhaust gas compressor 423 as shown. The NG vaporized through the heat exchange operation in the second heat exchanger 450 flows into the third heat exchanger 470.

Therefore, the exhaust gas is further cooled while passing through the third heat exchanger 470, and the LNG introduced into the first condenser 460 passes through the second heat exchanger 450 and the third heat exchanger 470 and finally reaches zero. Vaporized NG with a temperature around < RTI ID = 0.0 > In addition, the vaporized NG may be supplied to the demand source as shown in FIG. 1, or may be supplied to the burner 220, and the exhaust gas discharged through the third heat exchanger 470 may be a third exhaust gas cooler ( 433).

On the other hand, the pure oxygen combustion type vaporization apparatus 1 according to the present embodiment may further include an oxygen supply amount adjusting means for adjusting the flow rate of oxygen supplied to the burner 220 so that the combustion is completely burned.

As shown in FIG. 4, the oxygen supply amount adjusting means may include a solenoid valve 610, an oxygen sensor 620, and a controller 630.

The solenoid valve 610 is provided on the flow path connecting the oxygen holder 362 and the burner 220 to adjust the flow rate of oxygen supplied from the oxygen holder 362 to the burner 220.

The solenoid valve 610 is controlled by the control unit 630, the control unit 630 is a detection signal of the oxygen sensor 620 to check the oxygen amount by measuring the partial pressure of oxygen in the exhaust gas discharged from the LNG vaporization means 200 It receives the input to control the operation of the solenoid valve 610.

The oxy-fuel type vaporization apparatus 1 according to the present embodiment may further be adjusted to realize complete combustion in the burner 220 by further including an oxygen supply amount adjusting means, whereby by the oxygen production means 300. Unnecessary consumption of the produced oxygen can be prevented.

Pure oxygen combustion type vaporization apparatus 1 according to an embodiment of the present invention, by including the oxygen production means 300, it is possible to improve the combustion efficiency by performing the pure oxygen combustion in the burner 220, Through this, the amount of carbon dioxide discharged from the LNG vaporization means 200 can be reduced.

In addition, the oxy-fuel type vaporization apparatus 1 according to an embodiment of the present invention includes a carbon dioxide liquefaction means 400 and a liquefied carbon dioxide storage means 500, so that it is easy to discharge from exhaust gas discharged by pure oxygen combustion. By collecting and storing carbon dioxide, it is possible to prevent carbon dioxide from being released into the air.

As the present invention can be variously modified by those skilled in the art without departing from the scope of the claims claimed in the claims, the protection scope of the present invention is limited to the specific preferred embodiments described above It doesn't work.

One; Pure oxygen combustion vaporizer 100; LNG storage means
110; Pump 200; LNG vaporization means
210; Countertop 220; burner
230; First heat exchanger 300; Oxygen production
310; Air filter 320; Air compressor
321; Regression 322; valve
330; Air cooler 340; Water separator
350; Adsorption tower 351; Solenoid valve
360; Oxygen storage means 361; Buffer tank
362; Oxygen holder 370; Vacuum pump
380; Silencer 400; CO2 Liquefaction Means
410; Water separator 421,422,423; Exhaust gas compressor
431,432,433; Exhaust cooler 440; Molecular filter
450; Second heat exchanger 460; Condenser
470; Third heat exchanger 500; Liquefied Carbon Dioxide Storage
610; Solenoid valve 620; Oxygen sensor
630; The control unit

Claims (13)

LNG storage means for storing LNG (Liquefied Natural Gas);
A water tank, a burner provided in the water tank and the fuel gas is combusted so that the water in the water tank is heated, and the LNG provided in the water tank and supplied from the LNG storage means passes and exchanges heat with the heated water in the water tank. LNG vaporization means comprising a first heat exchanger to be vaporized;
Oxygen production means for producing oxygen and supplying oxygen to the burner;
Carbon dioxide liquefaction means for collecting and liquefying carbon dioxide from the exhaust gas discharged from the LNG vaporization means; And
And liquefied carbon dioxide storage means for storing carbon dioxide liquefied by the carbon dioxide liquefaction means.
The method according to claim 1,
The fuel gas is a oxy-fuel combustion vaporizer, characterized in that the natural gas (NG) vaporized by the LNG vaporization means.
The method according to claim 2,
The oxygen production means,
An air filter for filtering air introduced from the outside;
An air compressor for compressing air passing through the air filter;
An adsorption tower into which the compressed air is introduced from the air compressor, and the zeolite is filled therein so that nitrogen is adsorbed and oxygen is permeated and discharged from the introduced air; And
And oxygen storage means for storing oxygen discharged from the adsorption tower and connected to the burner so that oxygen is supplied to the burner.
The method according to claim 3,
The oxygen production means,
An air cooler for cooling the compressed air in the air compressor; And
And a water separator connected to the adsorption tower such that water in the air cooled by the air cooler is separated, so that gaseous air is supplied to the adsorption tower.
The method according to claim 3,
The oxygen storage means,
A buffer tank storing oxygen discharged from the adsorption tower; And
And an oxygen holder for receiving oxygen from the buffer tank and storing the oxygen after supplying the oxygen to the burner.
The method according to claim 5,
And an oxygen supply amount adjusting means for adjusting a flow rate of oxygen supplied from the oxygen holder to the burner.
The method of claim 6,
The oxygen supply amount adjusting means,
A solenoid valve controlling a flow rate of oxygen supplied from the oxygen holder to the burner;
An oxygen sensor for measuring the amount of oxygen in the exhaust gas discharged from the LNG vaporization means; And
And a control unit for receiving the detection signal of the oxygen sensor to control the operation of the solenoid valve.
The method according to any one of claims 3 to 7,
The oxygen production means,
And a vacuum pump connected to the adsorption tower and configured to decompress the inside of the adsorption tower to separate nitrogen adsorbed from the adsorption tower and to discharge the adsorption tower from the adsorption tower.
The method according to claim 8,
The oxygen production means,
Pure oxygen combustion type vaporization characterized in that it further comprises; a silencer connected to the vacuum pump so that the nitrogen discharged through the vacuum pump from the adsorption tower to the outside, the noise generated by the vacuum pump is removed; Device.
The method according to claim 2,
The carbon dioxide liquefaction means,
An exhaust gas compressor generated after combustion of the fuel gas to exhaust the exhaust gas discharged from the LNG vaporization means;
An exhaust gas cooler configured to cool the exhaust gas compressed by the exhaust gas compressor;
A molecular filter (Molecular Sieve (MS)) which allows the remaining carbon dioxide to be discharged after the water molecules are separated from the exhaust gas cooled by the exhaust gas cooler; And
And a heat exchange means for allowing the carbon dioxide discharged from the molecular filter to be liquefied while being heat-exchanged and discharged to the liquefied carbon dioxide storage means.
The method of claim 10,
The heat exchange means,
A condenser through which a heat exchange medium supplied from the outside passes; And
A second heat exchanger passing through the heat exchange medium discharged from the condenser, and heat exchanged with the heat exchange medium while passing carbon dioxide discharged from the molecular filter;
The carbon dioxide having passed through the second heat exchanger is liquefied as it is heat exchanged with the heat exchange medium supplied to the condenser and supplied to the condenser from the outside, oxy-combustion type vaporization apparatus.
The method of claim 11,
The carbon dioxide liquefaction means,
The heat exchange medium connected to the second heat exchanger passes through the heat exchange medium discharged from the second heat exchanger, and the heat exchange medium connected to the exhaust gas compressor and the exhaust gas cooler passes through the exhaust gas discharged from the exhaust gas compressor. And a third heat exchanger configured to be supplied to the exhaust gas cooler after heat exchange with the exhaust gas cooler.
The method of claim 12,
And the heat exchange medium supplied to the condenser is LNG discharged from the LNG storage means.

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