KR102086641B1 - Medium Carburetor - Google Patents

Abstract

The intermediate medium vaporizer has an intermediate medium evaporator for evaporating at least a portion of the intermediate medium by heat exchange between the first heat source medium and the liquid intermediate medium, and a heat transfer tube into which a low temperature liquefied gas having a pressure of 6 MPaG or more is introduced. By condensing the intermediate medium evaporated in the intermediate medium evaporator, a liquefied gas vaporizer which vaporizes the low temperature liquefied gas in the heat transfer pipe and outflows the gas, and a heater that heats the gas discharged from the liquefied gas vaporizer by the second heat source medium. Equipped. The first heat source medium is sea water or air, the second heat source medium is steam or hot water, and the warmer is constituted by a micro channel heat exchanger.

Description

Medium Carburetor

The present invention relates to an intermediate media vaporizer.

Conventionally, as disclosed in Patent Document 1 below, as an apparatus for vaporizing low temperature liquid such as LNG (Liquefied Natural Gas), an intermediate medium vaporizer using an intermediate medium in addition to a heat source fluid is known. As shown in FIG. 5, the intermediate medium vaporizer disclosed in Patent Document 1 includes an intermediate medium evaporator 81, an LNG evaporator 82, and a heater 83.

In addition, the inlet chamber 85, the plurality of heat transfer tubes 86, the intermediate chamber 87, the plurality of heat transfer tubes 88 and the outlet chamber 89 are in this order as a path through which the seawater as the heat source fluid passes through the vaporizer. It is installed. The heat transfer tubes 86 are arranged in the warmer 83 and the heat transfer tubes 88 in the intermediate medium evaporator 81, respectively.

In the intermediate medium evaporator 81, an intermediate medium (for example, propane) M having a boiling point lower than the temperature of seawater is accommodated.

The LNG evaporator 82 includes an inlet chamber 91 and an outlet chamber 92, and a plurality of heat transfer tubes 93 communicating with both chambers 91 and 92. Each heat pipe 93 is substantially U-shaped and protrudes upwards in the intermediate medium evaporator 81. The outlet chamber 92 communicates with the heater 83 via the NG conduit 94.

In such a vaporizer, seawater, which is a heat source fluid, reaches the outlet chamber 89 through the inlet chamber 85, the heat transfer tube 86, the intermediate chamber 87, and the heat transfer tube 88, and passes through the heat transfer tube 88. The seawater exchanges heat with the liquid intermediate medium M in the intermediate medium evaporator 81 to evaporate the intermediate medium M.

On the other hand, LNG to be vaporized is introduced into the heat transfer tube 93 from the inlet chamber 91. By the heat exchange between the LNG in the heat transfer tube 93 and the evaporation intermediate medium in the intermediate medium evaporator 81, the intermediate medium M condenses, the heat of condensation is received, and the LNG evaporates into the heat transfer tube 93, NG (Natural Gas). This NG is introduced into the warmer 83 from the outlet chamber 92 through the NG conduit 94 and further heated by heat exchange with seawater flowing through the heat transfer pipe 86 in the warmer 83. It is supplied to the use side.

Japanese Patent Laid-Open No. 2000-227200

In the intermediate | middle medium vaporizer | carburetor disclosed by patent document 1, the heater 83 has the structure which has many heat exchanger tubes 86. As shown in FIG. For this reason, there is a limit to downsizing the warmer 83, and inevitably there is a limit to downsizing the intermediate medium vaporizer itself. In particular, when high-pressure LNG is introduced into the intermediate medium vaporizer, the pressure in the heater 83 also increases, so that pressure resistance is also required for the heat transfer tube 86 and the tube plate and shell included therein, thereby providing proper pressure resistance performance. In order to realize this, further miniaturization becomes difficult.

Then, this invention is made | formed in view of the said prior art, The objective is to provide the intermediate | middle medium-type vaporizer which can aim at miniaturization.

In order to achieve the above object, an intermediate medium vaporizer provided as one embodiment of the present invention includes an intermediate medium evaporator for evaporating at least a portion of the intermediate medium by heat exchange between the first heat source medium and the liquid medium. A liquefied gas vaporizer having a heat transfer tube into which a low temperature liquefied gas having a pressure of 6 MPaG or more is introduced and vaporizing the low temperature liquefied gas in the heat transfer tube by condensing the intermediate medium evaporated in the intermediate medium evaporator; It is an intermediate | middle medium type | mold vaporizer provided with the warmer which heats the said gas which flowed out from the liquefied gas vaporization part with a 2nd heat source medium. The first heat source medium is sea water or air, the second heat source medium is steam or hot water, and the warmer is constituted by a micro channel heat exchanger.

BRIEF DESCRIPTION OF THE DRAWINGS It is a figure which shows roughly the structure of the intermediate | middle media type | mold vaporizer which concerns on 1st Embodiment.
FIG. 2 is a diagram schematically showing the configuration of a heater provided in the intermediate medium vaporizer in a partially broken state. FIG.
It is a figure which partially enlarges and shows the laminated body installed in the warmer.
4 is a diagram schematically showing a configuration of an intermediate media vaporizer according to a second embodiment.
Fig. 5 is a view schematically showing the configuration of a conventional intermediate medium vaporizer.

EMBODIMENT OF THE INVENTION Hereinafter, embodiment is described in detail, referring drawings.

(1st embodiment)

As shown in FIG. 1, the intermediate | middle medium type | mold vaporizer (henceforth a vaporizer | carburetor) 10 which concerns on 1st Embodiment liquefyes heat of the seawater which is a 1st heat source medium through intermediate | middle medium M at low temperature. It is a device that delivers gas to liquefied natural gas (LNG) and vaporizes LNG to obtain gas. The vaporizer 10 may be configured as a device for vaporizing or warming low-temperature liquefied gas other than LNG, such as liquefied petroleum gas (LPG), liquid nitrogen (Liquid Nitrogen, LN ² ), and the like.

The vaporizer | carburetor 10 is equipped with the intermediate medium evaporator E1 which is an intermediate | middle medium evaporator, the LNG evaporator E2 which is a liquefied gas vaporizer, and the warmer E3. The intermediate medium evaporator E1 and the LNG evaporator E2 are provided in one hollow casing 11.

The casing 11 has a long shape in the horizontal direction, the lower portion of which is configured as a casing portion (first casing portion) of the intermediate medium evaporator E1, and the upper portion of the casing portion (second casing portion) of the LNG evaporator E2. It is configured as.

An inlet chamber (water chamber) 14 is adjacent to one of the pair of side walls constituting the first casing part, and an outlet chamber 18 is adjacent to the other (other surface). In the intermediate medium evaporator E1, a plurality of heat transfer tubes 20 are provided. The heat exchanger tube 20 is arrange | positioned under the space in the casing 11. The heat exchanger tube 20 serves as a partition wall between the first side wall 11a which functions as a partition wall with the inlet chamber 14 and the outlet chamber 18 among a pair of sidewalls constituting the first casing part. It spans between the functioning 2nd side walls 11b. The heat transfer tube 20 has a shape extending in a straight line in one direction, but is not limited to this shape.

Inlet chamber 14 is connected to inlet chamber 14, in which a pump or the like not shown is provided, and seawater from the sea is introduced into inlet chamber 14 through inlet tube 22. That is, the seawater before being introduced into the entrance chamber 14 is not used to warm NG (Natural Gas).

A discharge pipe 24 for discharging sea water is connected to the outlet chamber 18. Seawater in the outlet chamber 18 is discharged to the outside through the discharge pipe 24.

In the casing 11, an intermediate medium (for example, propane) M having a boiling point lower than the temperature of seawater is accommodated. The intermediate medium M is accommodated so that a liquid level may be located above all the heat transfer tubes (heat transfer tubes through which seawater flows) 20.

Above the outlet chamber 18, the inlet chamber 32 of LNG and the outlet chamber 34 which derives NG are provided. The entrance chamber 32 and the exit chamber 34 are adjacent to the outer side in the upper side of the 2nd side wall 11b. The exit chamber 34 is formed adjacent to the upper side of the entrance chamber 32. The inlet chamber 32 is connected with a supply pipe 36 for introducing LNG. The outlet pipe 34 for connecting NG is connected to the outlet chamber 34. LNG having a pressure of 6 MPaG or more (6 MPa in gauge pressure) is introduced into the inlet chamber 32.

The LNG evaporator E2 includes the inlet chamber 32, the outlet chamber 34, and a plurality of heat transfer tubes 40 communicating with the inlet chamber 32 and the outlet chamber 34. Each heat pipe 40 has a substantially U shape, the first end is connected to the inlet chamber 32, and the second end is connected to the outlet chamber 34. The heat transfer tube 40 is disposed above the heat transfer tube 20 in the casing 11, that is, above the liquid level of the intermediate medium M.

Warmer E3 is connected to the lead-out pipe 38. NG is supplied to the warmer E3 through the lead-out pipe 38, heated in the warmer E3, and then supplied to the use side.

The warmer E3 is comprised by the microchannel heat exchanger provided with the laminated body of the structure by which the many metal plates 43 and 44 which were excellent in the heat transfer characteristic shown in FIG. 3 were laminated | stacked. Specifically, as shown in FIGS. 2 and 3, in the microchannel heat exchanger, the laminate of the metal plates 43 and 44 is sandwiched between the end plates 45 and 45. Is a first metal plate 43 in which a plurality of flow paths (first flow path) 43a through which NG flows is concave, and a plurality of flow paths (second flow path) 44a through which steam as the second heat source medium flows are formed. The two metal plates 44 are laminated | stacked alternately. And heat exchange is performed between NG which flows in each 1st flow path 43a, and steam which flows in each 2nd flow path 44a, and NG is heated. The flow path formed in these metal plates 43 and 44 has the flow path width of 0.2 mm-3 mm, for example. In addition, hot water may be used instead of steam as the second heat source medium.

NG flows through each of the first flow paths 43a, and steam such as water vapor as a second heat source medium flows through each of the second flow paths 44a. The second heat source medium may be a heat source medium different from the first heat source medium (sea water in this embodiment), and may be, for example, hot water.

The first inflow header 47 and the first outflow header 48 communicate with each of the first flow paths 43a, and the second inflow header 49 and the second flow paths with each of the second flow paths 44a. The outflow header 50 is in communication. The NG supplied through the discharge pipe 38 is distributed to each of the first flow paths 43a through the first inflow header 47, and the NG flowing through each of the first flow paths 43a is the first outflow header 48. And are derived from the warmer (E3). The steam supply pipe 51 is connected to the second inflow header 49. Steam supplied through this supply pipe 51 is distributed to each of the second flow paths 44a through the second inflow header 49, and steam flowing through each of the second flow paths 44a is the second outflow header 50. ), Derived from the warmer (E3).

Here, the operation | movement operation of the vaporizer | carburetor 10 which concerns on 1st Embodiment is demonstrated.

The liquid intermediate medium M stored in the lower part of the casing 11 is heated and evaporated by the seawater which flowed into each heat pipe 20 through the inlet chamber 14. That is, in the heating medium evaporator E1, the intermediate medium M is heated by the first heat source medium and evaporated. The evaporated intermediate medium M heats the heat exchanger tube 40 located in the upper part of the casing 11. The LNG which flows into the heat exchanger tube 40 from the supply pipe 36 through the inlet chamber 32, and flows into the heat exchanger tube 40 is heated and evaporated by the heat exchanger tube 40, and becomes NG. In addition, seawater flows out from the heat transfer pipe 20 and is discharged to the outside through the outlet chamber 18 and the discharge pipe 24.

NG flows through the outlet pipe 38 via the outlet chamber 34 and is introduced into the warmer E3. In the warmer E3, NG is classified into each 1st flow path 43a via the 1st inflow header 47. As shown in FIG. The NG flowing in each of the first flow paths 43a is heated by steam flowing in each of the second flow paths 44a, is led out of the warmer E3 through the first outflow header 48, and supplied to the use side. .

As described above, in the present embodiment, since the heater E3 is constituted by a microchannel heat exchanger, the size of the heater E3 is reduced compared with the case where the heater is constituted by a shell and tube type heat exchanger. We can plan.

In addition, the vaporizer 10 itself can be miniaturized. In particular, LNG having a pressure of 6 MPaG or more (6 MPa at the gauge pressure) is introduced into the LNG evaporator E2. Even when vaporizing such high pressure LNG, since the heater E3 is comprised by the microchannel heat exchanger, like the conventional intermediate | middle medium type | system | group vaporizer shown in FIG. 5, the heat exchanger tube, the tube plate, and the shell of the heater E3. It is not necessary to take measures to increase the pressure resistance performance by increasing the thickness of.

Therefore, it is possible to prevent the heater E3 from being enlarged while being configured to vaporize high-pressure LNG. In addition, since the heater E3 can be downsized, the heater E3 can be reduced in weight.

In addition, since the heater E3 is constituted by a microchannel heat exchanger, like the heater E3 of the intermediate medium vaporizer, it does not have an outer shell and a can plate, and has a high pressure in the direction in which the heat transfer tube is compressed from the outside. Since there is no structure to endure, even when a high pressure gas is introduce | transduced into the warmer E3, the warmer E3 does not become large. In addition, in the configuration of Fig. 5, in addition to the large size and the mass of the apparatus, it is difficult to achieve the desired NG outlet temperature in the sea water cryogenic phase.

In addition, in this embodiment, since steam is used as a 2nd heat source medium, compared with the case where seawater or air is used as a 2nd heat source medium, the heating performance of the gas in the warmer E3 can be made high. Moreover, even in a cold region, the gas of the temperature requested | required from a utilization side can be obtained.

Moreover, in this embodiment, there also exists an effect of driving cost reduction. This point is demonstrated concretely below. The driving cost required in the case of the configuration of the present embodiment is referred to as A, and the driving cost required in the case of the all-steam heat source vaporizer in which the first heat source medium also uses steam is referred to as B, and the driving cost is compared throughout the year. .

The heat load distribution in the intermediate medium evaporator E1 and the heater E3 of the total amount of vaporization heat (100%) in the vaporizer is generally about 80% and about 20%, respectively. In this embodiment, 80% of the heat load is supplied by inexpensive natural energy (sea water), and the remaining 20% is provided by expensive steam. On the other hand, in all steam heat source vaporizers, 100% of heat load is supplied by expensive steam (about 90% of fuel thermal efficiency).

Since the required unit of pump power (electric power) is about 4 KWh / t-LNG, when the power unit price is 10 yen / KWh, 40 yen is required to vaporize 40 yen / t-LNG, that is, LNG-1ton. On the other hand, since the unit of steam (fuel cost) source consumes approximately 1.5% (when the thermal efficiency is 90%) based on the fuel consumption amount, and becomes 15 Kg / t-LNG, in this case, the fuel gas unit price including gasification cost Is 40,000 yen / t, it costs 600 yen to vaporize 600 yen / t-LNG, or LNG-1ton.

In the vaporizer | carburetor 10 which concerns on this embodiment, since the intermediate | middle medium evaporator (E1): 80% and the heater (E3): 20% of heat load distribution, operation cost A is 40 * 0.8 + 600 * 0.2 = 152 yen / t-LNG. On the other hand, since the driving cost B in all the steam heat source vaporizers becomes a 100% steam heat source, it becomes 600 yen / t-LNG. Therefore, the driving expenses are clearly A << B.

Furthermore, in the year-end, in the vaporizer | carburetor 10 which concerns on this embodiment, in summer, the heat load in the intermediate medium evaporator E1 becomes large and the heat load in the warmer E3 becomes small by rising seawater temperature. As a result, the driving cost A is reduced. On the other hand, in all steam heat source vaporizers, even if the heat load in the intermediate | middle medium evaporator E1 became large, operating cost B is not reduced.

In the case where partial load operation is unavoidable in operation, in the vaporizer 10 of the present embodiment, the heat load in the intermediate medium evaporator E1 is large and the heat load in the warmer E3 is small. For this reason, the driving cost A may be reduced in excess of the partial load rate.

On the other hand, in all steam heat-type warmers, the running cost B does not exceed this and reduces it as it is with partial load ratio. Since changes in seawater temperature and partial load operation are inevitable, in the year-round unemployment industry, the difference in operating expenses over the year is further enlarged to A <<< B due to the above-described synergistic effect.

(2nd embodiment)

4 schematically shows a configuration of the vaporizer 10 according to the second embodiment. As shown in FIG. 4, in the second embodiment, unlike the first embodiment, air is used as the first heat source medium. In addition, only the structure and effect different from 1st Embodiment are demonstrated here.

In the first embodiment, the intermediate medium evaporator E1 and the LNG evaporator E2 are configured in the common casing 11, but in the second embodiment, the intermediate medium evaporator E1 and the LNG evaporator E2 are provided. Is composed separately.

The LNG evaporator E2 is provided with the housing 55 in which the intermediate | middle medium M was enclosed, and the heat exchanger tube 40 arrange | positioned in this housing 55 and vaporizing LNG. The housing 55 is provided with an inlet chamber 32 through which LNG is introduced and an outlet chamber 34 through which NG flows out. In the lower part of the housing 55, a liquid reservoir 55a for storing the intermediate medium M is provided.

The circulation path 57 of the intermediate medium M is connected to the housing 55. One end of the circulation passage 57 is connected to the lower surface of the liquid reservoir 55a in the housing 55 and extends outside the housing 55. The other end of this circulation path 57 is connected to the upper surface part of the housing 55. The pump 58 is provided in the circulation path 57, and the intermediate medium M stored in the liquid reservoir 55a flows in the circulation path 57 by driving the pump 58.

In the middle part of the circulation path 57, the heat exchanger tube 20 of the intermediate medium evaporator E1 is connected. Therefore, the circulation path 57 is the liquid pipe 57a through which the liquid intermediate medium M flows toward the heat transfer pipe 20, and the intermediate medium M in the gaseous state by evaporating from the heat transfer pipe 20 toward the LNG evaporator E2. ) Includes a gas pipe 57b flowing therethrough.

The intermediate medium evaporator E1 is a structure in which the heat exchanger tube 20 is arrange | positioned in the heat exchange chamber 60 into which air | atmosphere is introduce | transduced. The blower chamber 61 is provided above the heat exchange chamber 60, and the air | atmosphere flows into the heat exchange chamber 60 via the blower chamber 61 by driving the blower 62. FIG. In the present embodiment, the air flows from the top to the bottom, but the air may flow from the bottom to the top. In addition, the blower chamber 61 may be abbreviate | omitted and the blower 62 may be provided in the heat exchange chamber 60, and the atmosphere may be introduce | transduced into the heat exchange chamber 60 directly. Moreover, the structure which air | atmosphere flows toward the blower chamber 61 from the heat exchange chamber 60 may be sufficient.

In the second embodiment, the liquid intermediate medium M stored in the liquid reservoir 55a in the housing 55 flows through the liquid pipe 57a of the circulation passage 57 when the pump 58 is driven. It is introduced into the heat exchanger tube 20 of the evaporator E1. In the heat transfer tube 20, the intermediate medium M is heated by the atmosphere to evaporate, and flows through the gas pipe 57b of the circulation path 57. This gaseous intermediate medium M is introduced into the housing 55 of the LNG evaporator E2 to heat the heat transfer tube 40. As a result, the LNG in the heat transfer pipe 40 is vaporized to become NG. NG is introduced into the warmer E3 through the lead pipe 38, heated by steam, and then supplied to the use side.

[Schematic description of embodiment]

From the above 1st Embodiment and the said 2nd Embodiment, the intermediate | middle medium type | system | group vaporizer provided as one form of this invention is demonstrated schematically.

An intermediate medium vaporizer, which is provided as one embodiment of the present invention, includes an intermediate medium evaporator for evaporating at least a portion of the intermediate medium by heat exchange between a first heat source medium and a liquid intermediate medium, and a low temperature having a pressure of 6 MPaG or more. A liquefied gas vaporizer having a heat transfer tube into which the liquefied gas is introduced, and condensing the intermediate medium evaporated in the intermediate medium evaporator to vaporize the low temperature liquefied gas in the heat transfer tube, and outflow the gas; And a heater for heating the gas by the second heat source medium. The first heat source medium is sea water or air, the second heat source medium is steam or hot water, and the warmer is constituted by a micro channel heat exchanger.

In this intermediate medium vaporizer, since the heater is constituted by the microchannel heat exchanger, the heater can be miniaturized as compared with the case where the heater is constituted by the shell-and-tube type heat exchanger.

In addition, the intermediate medium vaporizer itself can be miniaturized. In particular, a low temperature liquefied gas having a pressure of 6 MPaG (6 MPa at a gauge pressure) or higher is introduced into the liquefied gas vaporization unit. Even when vaporizing such a high pressure low temperature liquefied gas, since the heater is composed of a microchannel heat exchanger, it is not necessary to take measures to increase the pressure resistance performance by increasing the thickness of the heat transfer tube, the tube plate and the shell.

Therefore, the heater can be prevented from being enlarged while being configured to vaporize the high pressure low temperature liquefied gas.

In addition, the heater can be miniaturized, and the weight of the heater can be reduced. In addition, since the second heat source medium is steam or hot water, the heating performance by the warmer can be increased as compared with the case where seawater or air is used as the second heat source medium.

Moreover, even in a cold region, the gas of the temperature requested | required from a utilization side can be obtained.

Here, a microchannel heat exchanger is a heat exchanger provided with the laminated body of the structure by which the many metal plate which was excellent in the heat transfer property was laminated | stacked. This laminated body has the structure which the metal plate in which the flow path which a gas flows in is concave, and the metal plate in which the flow path which a 2nd heat source medium flows in are recessed laminated alternately. The flow path formed in these metal plates has the flow path width of 0.2 mm-3 mm, for example. For this reason, even when a high-pressure gas is introduced into the warmer, it is not necessary to redesign the warmer for high withstand pressure, and the warmer does not increase in size.

As described above, the intermediate medium vaporizer can be miniaturized.

Claims (3)

An intermediate medium evaporator for evaporating at least a portion of the intermediate medium by heat exchange between a first heat source medium and a liquid intermediate medium;
A liquefied gas vaporizer having a heat transfer tube into which a low temperature liquefied gas having a pressure of 6 MPaG or more is introduced, and vaporizing the low temperature liquefied gas in the heat transfer tube by condensing the intermediate medium evaporated in the intermediate medium evaporator;
A heater for heating the gas flowing out of the liquefied gas vaporization unit by a second heat source medium,
The first heat source medium is sea water or air, the second heat source medium is steam or hot water,
The heater is constituted by a micro channel heat exchanger,
Medium Carburetor. The method of claim 1,
The liquefied gas vaporizer includes a housing in which the intermediate medium is sealed, and the heat transfer tube is disposed in the housing. The method according to claim 1 or 2,
The intermediate medium evaporation unit,
A heat exchange chamber into which the first heat source medium made of air is introduced, from one side of which the heat transfer tube into which the intermediate medium is introduced is disposed;
And a blower chamber provided with a blower for sending air to the heat exchange chamber.

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