Patent Description:
A condenser-evaporator in a nitrogen production device which mainly produces nitrogen exchanges heat between nitrogen gas from an overhead of a distillation column which concentrates nitrogen from air and oxygen enriched liquid air from a bottom of a distillation column, and the nitrogen gas is condensed to produce a reflux fluid in the distillation column.

With the condensation of the nitrogen gas, the oxygen enriched liquid air, which is a refrigerant, evaporates, and a part of it is used to generate cold in the nitrogen production device. In addition, another part of it is used as a part of raw material air or as a raw material of a second distillation column in order to improve the recovery rate of nitrogen.

As such a condenser-evaporator, a condenser-evaporator using a plate fin-type heat exchanger core is usually used. This type of condenser-evaporator has a form in which the heat exchanger core is immersed in the liquid reservoir (liquid storage-type) and a form in which the heat exchanger core is not immersed (dry-type).

In the dry-type condenser-evaporator, oxygen enriched liquid air is supplied into the heat exchange core via a header and completely gasified by heat exchange with nitrogen gas and led out. Therefore, a nitrogen concentration of the led-out gas is equal to a nitrogen concentration of the supplied oxygen enriched liquid air.

On the other hand, in the liquid storage-type condenser-evaporator, the oxygen enriched liquid air stored in the container flows in from the bottom of the heat exchange core immersed by the thermosiphon effect, partly evaporates, and flows out from an upper part of the core in a gas-liquid two-phase state. The evaporated gas is removed from the container and the non-evaporated liquid is returned to the container.

As a result, a nitrogen concentration of the oxygen enriched liquid air led out from a bottom of the container becomes smaller than that of the supplied oxygen enriched liquid air, and a nitrogen concentration of the evaporated gas led out from the container increases. In this way, in the liquid storage-type condenser-evaporator, it is possible to separate the components of the supplied oxygen enriched liquid air.

However, since the oxygen enriched liquid air in the container is led out in the liquid-storage type condenser-evaporator, the amount of nitrogen in the evaporated gas is smaller than that in the dry-type condenser-evaporator. Even if the evaporated gas is used as a part of the raw material air or as a raw material of the second distillation column, the nitrogen recovery rate cannot be improved.

In order to solve such a problem, it is conceivable to use a multistage liquid storage-type condenser-evaporator. For example, <CIT> (also published as <CIT>) discloses a multistage liquid storage-type condenser-evaporator including an evaporation passage partitioned into a plurality of stages and a liquid storage section for storing liquid supplied and led out into the evaporation passage.

The action of the multistage liquid storage-type condenser-evaporator disclosed in <CIT> is as follows.

When oxygen enriched liquid air is supplied into a top liquid storage section of the multistage liquid storage-type condenser-evaporator including an evaporation area with two stages, the oxygen enriched liquid air stored in the liquid storage section flows into an evaporation passage from a lower evaporation inflow passage, and the liquid level becomes the same in the liquid storage section and in the evaporation passage.

When nitrogen gas passes through a condensation passage in this state, heat exchange is performed, a part of the oxygen enriched liquid air evaporates to form a gas-liquid two-phase, an ascending flow is generated by the thermosiphon effect, and the oxygen enriched liquid air in a gas-liquid two-phase is led out from the upper evaporation outflow passage as a gas-liquid two-phase. The led-out gas is taken out from an evaporated gas outlet of the liquid storage section. On the other hand, the liquid that has not evaporated returns into the liquid storage section, and a circulating flow is formed between the liquid storage section and the evaporation passage. Due to the evaporation and circulation at this time, the nitrogen concentration of the evaporated gas increases, and the nitrogen concentration of the oxygen enriched liquid air stored in the liquid storage section decreases.

When the liquid level in the liquid storage section rises above the liquid level in the communication introduction passage, the oxygen enriched liquid air with reduced nitrogen concentration flows into the communication passage from the communication introduction passage and is led out from the communication outflow passage, and stored in the next lower liquid storage section. In this stage as well, the oxygen enriched liquid air is evaporated and circulated, and a gas having a lower nitrogen concentration than that of the gas in the upper stage is led out. In this way, two types of gases having different nitrogen concentrations can be produced. The nitrogen recovery rate can be increased by using the evaporative gas having a high nitrogen concentration as a part of the raw material air or as a raw material of the second distillation column.

However, the nitrogen concentration of the oxygen enriched liquid air stored in the bottom liquid storage section is about <NUM>% or less. This decrease in nitrogen concentration raises the boiling point of oxygen enriched liquid air. Therefore, the temperature difference between the fluid flowing in the bottom evaporation passage and the nitrogen flowing in the condensation passage becomes small. Therefore, it is desired to increase the temperature difference in the bottom stage.

In addition, in order to make the multistage liquid storage-type condenser-evaporator compact, if the pressure of the oxygen enriched liquid air supplied into the top liquid storage section is reduced, there is a problem in that the power for producing nitrogen increases.

<CIT> discloses a bath condenser with a condenser block that has evaporation passages for a liquid and liquefaction passages for a heating medium. The condenser block has at least two circulation sections that are located on top of one another, the evaporation passages each having on the lower end of a circulation section at least one entry opening for the liquid and on the upper end of the circulation section at least one exit opening. Only exit openings and entry openings that are located on the same side of the condenser block are connected via means for routing the liquid.

<CIT> discloses a main liquid medium supply means to a sump which comprises a main flow passage and a liquid supply hole designed to supply a liquid medium quantity to be set during a steady operation of a condensation vaporizer and a sub-liquid medium supply means which comprises a sub-flow passage and a liquid supply hole designed to replenish a liquid medium quantity equivalent to an increase in the amount of evaporation when the thermal load of the condensation vaporizer is further increased, are provided.

The present invention has been made to solve such a problem, and an object of the present invention is to provide a compact multistage liquid storage-type condenser-evaporator capable of producing two kinds of gases having different compositions without increasing power, and a nitrogen production device using the multistage liquid storage-type condenser-evaporator without increasing the power for producing nitrogen.

According to a first aspect, there is provided a multistage liquid storage-type condenser-evaporator including:.

The multistage liquid storage-type condenser-evaporator may further include:.

The multistage liquid storage-type condenser-evaporator may further include a gas-liquid collection container which is configured to collect the gas which is flowed into the circulation liquid storage section and also serve as the bottom liquid storage section, and the gas-liquid collection container includes a liquid inlet which is configured to introduce liquid from the outside into a top circulation liquid storage section, an evaporated gas outlet which is configured to lead out collected evaporated gas, and a liquid outlet which is configured to lead out stored liquid.

The multistage liquid storage-type condenser-evaporator may further include a conduit which is configured to supply liquid led out through the liquid outlet into a bottom evaporation passage, and a decompressor provided in the conduit.

The heat exchanger core may be made of a heat exchange section and a liquid communication section, the liquid communication section includes the communication passage and the bottom communication passage, and the liquid communication section is provided on at least one side of the heat exchange section in the stacking direction of the condensation passage and the evaporation passage forming the heat exchange section.

According to a second aspect, there is provided a nitrogen production device including a multistage liquid storage-type condenser-evaporator, first and second distillation columns in which a mixed fluid of oxygen, nitrogen and argon is separated by cryogenic distillation, and an expansion turbine,.

According to a third aspect, there is provided a nitrogen production device including a multistage liquid storage-type condenser-evaporator, a distillation column in which a mixed fluid of oxygen, nitrogen and argon is separated by cryogenic distillation, and an expansion turbine,.

The multistage liquid storage-type condenser-evaporator according to the present invention includes the bottom liquid storage section which is configured to store the liquid supplied into the bottom evaporation passage without circulating, and the fluid collection section which is configured to collect the fluid flowing out from the bottom evaporation passage and discharge to the outside without returning into the bottom liquid storage section. Therefore, the liquid does not circulate in the bottom liquid storage section, so that the nitrogen concentration in the liquid does not decrease as in the conventional condenser-evaporator. Compared with the case in which liquid circulates, the temperature difference between the temperature of the fluid in the bottom evaporation region and the nitrogen flowing through the condensation passage can be increased. As a result, it is possible to realize a compact multistage liquid storage-type condenser-evaporator which produces two types of gases having different compositions.

As shown in <FIG>, a multistage liquid storage-type condenser-evaporator <NUM> of the present embodiment includes a heat exchanger core <NUM> having a heat exchange section <NUM> and two liquid communication sections <NUM> provided on both side surfaces of the heat exchange section <NUM> in the stacking direction, a multi-stage circulation liquid storage section <NUM> formed on one side of the heat exchanger core <NUM> in the width direction (hereinafter, simply referred to as "the width direction of the heat exchanger core") orthogonal to the stacking direction of the heat exchange section <NUM>, a bottom liquid storage section <NUM> provided at the lower end of the heat exchanger core <NUM>, and a fluid collection section <NUM> which collects fluid flowing out from the bottom evaporation passage <NUM> and discharges the fluid to the outside without returning into the bottom liquid storage section <NUM>.

The stacking direction of the heat exchange section <NUM> means a direction in which the condensation passage <NUM> and the evaporation passage <NUM>, which form the heat exchange section <NUM>, are stacked. The stacking direction of the heat exchange section <NUM> is also the stacking direction of one liquid communication section <NUM>, the heat exchange section <NUM>, and the other liquid communication section <NUM>.

Further, the width direction of the heat exchanger core <NUM> is a direction orthogonal to the stacking direction. A plane formed by the stacking direction and the width direction of the heat exchanger core <NUM> is a horizontal plane with respect to the vertical direction of the multistage liquid storage-type condenser-evaporator.

Hereinafter, each configuration will be described in detail. In the following description, a case in which the multistage liquid storage-type condenser-evaporator <NUM> is used as a condenser-evaporator in a nitrogen production device which exchanges heat between nitrogen gas and oxygen enriched liquid air to condense nitrogen gas and evaporate the oxygen enriched liquid air will be explained as an example.

In the heat exchange section <NUM>, oxygen enriched liquid air and nitrogen gas are circulated and heat-exchanged with each other to condense the nitrogen gas and evaporate the oxygen enriched liquid air. The heat exchange section <NUM> is formed by stacking the condensation passage <NUM> and the evaporation passage <NUM> adjacent to each other. As shown in <FIG>, the heat exchange section <NUM> in the present embodiment is formed by stacking three condensation passages <NUM> and four evaporation passages <NUM>.

The condensation passage <NUM> and the evaporation passage <NUM> are a so-called plate fin type passage which is formed by laminating a plate (tube plate), fins (corrugated fins), sidebars, or the like, similarly to the multistage liquid storage-type condenser-evaporator disclosed in Patent Document <NUM>.

The condensation passage <NUM> is formed by using vertically oriented fins. As shown in <FIG>, the flow path of the condensation passage <NUM> is formed so as to communicate from the upper end surface to the lower end surface of the heat exchanger core <NUM>. Nitrogen gas flows in from the upper end of the condensation passage <NUM>, is cooled while passing through the inside of the condensation passage <NUM>, and is led out as liquid nitrogen from the lower end. At the lower end of the heat exchanger core <NUM>, a liquid nitrogen outlet (not shown) for leading out the liquid nitrogen condensed in the condensation passage <NUM> is provided.

As shown in <FIG>, the evaporation passage <NUM> is independently provided for each of the three evaporation areas of the first evaporation area to the third evaporation area. The evaporation passage <NUM> is formed by arranging fins (horizontal fins) along the width direction of the heat exchanger core <NUM> and fins (vertical fins) vertically so as to communicate with the horizontal fins.

As shown in <FIG>, the oxygen enriched liquid air stored in the circulation liquid storage section <NUM> flows in the evaporation inflow passage 17a which is the lower horizontal fins, ascends while evaporating along the vertical fins, flows in the evaporation outflow passage 17b which is the upper horizontal fins in the state of a gas-liquid two-phase fluid, and returned into the circulation liquid storage section <NUM>.

In addition, the oxygen enriched liquid air stored in the bottom liquid storage section <NUM> ascends in the bottom evaporation passage <NUM> while evaporating, almost all thereof evaporates to become evaporated gas, is collected in the fluid collection section <NUM> and led out to the outside.

As shown in <FIG>, a nitrogen gas header <NUM> for distributing and supplying nitrogen gas to a plurality of the condensation passages <NUM> is provided at the upper end of the heat exchanger core <NUM>, and the nitrogen gas header <NUM> is provided with a nitrogen gas introduction pipe 19a.

The liquid communication section <NUM> includes a communication passage <NUM> for flowing the liquid in the circulation liquid storage section <NUM> from the upper circulation liquid storage section <NUM> into the lower circulation liquid storage section <NUM>, and a bottom communication passage <NUM> for flowing the liquid in the bottom circulation liquid storage section <NUM> into the bottom liquid storage section <NUM>. The liquid communication section <NUM> is formed by plates and fins. The liquid communication section <NUM> is provided on both side surfaces of the heat exchange section <NUM> in the stacking direction of the heat exchange section <NUM>.

As shown in <FIG>, the communication passage <NUM> is provided on the side surfaces of the heat exchange section <NUM>, and the bottom communication passage <NUM> is provided further outside thereof.

In <FIG>, the liquid communication section is provided with double lines at a total of three places. This double line means that the liquid does not pass through it.

Further, the liquid communication section <NUM> of the present embodiment is formed by plates and fins, and is provided on both sides of the heat exchanger core <NUM> in the stacking direction. However, it is not essential that the liquid communication section <NUM> in the present invention be provided integrally with the heat exchanger core <NUM>. Apart from the heat exchanger core <NUM>, the liquid communication section <NUM> may be, for example, a pipe connecting each the circulation liquid storage section <NUM> and the bottom liquid storage section <NUM>.

The communication passage <NUM> is a passage for flowing the liquid in the circulation liquid storage section <NUM> in the first stage into the circulation liquid storage section <NUM> in the second stage. The bottom communication passage <NUM> is a passage for flowing the liquid in the circulation liquid storage section <NUM> at the bottom, that is, in this example, the circulation liquid storage section <NUM> in the second stage into the bottom liquid storage section <NUM>.

The circulation liquid storage section <NUM> is provided corresponding to the evaporation passage <NUM> of each stage except the evaporation passage at the bottom. The circulation liquid storage section <NUM> supplies liquid into the evaporation passage <NUM>, stores the liquid flowing out from the evaporation passage <NUM>, and circulates the liquid in the evaporation passage <NUM> of each stage.

The circulation liquid storage section <NUM> is provided on one side or both sides in the width direction of the heat exchanger core <NUM>.

The circulation liquid storage section <NUM> of the present embodiment is provided with an evaporated gas outlet 9a.

Further, the top circulation liquid storage section <NUM> is provided with a liquid inlet <NUM> for introducing oxygen enriched liquid air from the outside.

The bottom liquid storage section <NUM> is for supplying the liquid into the bottom evaporation passage <NUM>, and the liquid does not return from the bottom evaporation passage <NUM> into the bottom liquid storage section <NUM>. The bottom liquid storage section <NUM> is provided at the lower end of the heat exchanger core <NUM>. The bottom liquid storage section <NUM> is provided with a liquid outlet <NUM> for leading out the liquid to the outside.

The fluid collection section <NUM> collects the fluid (mainly evaporated gas) flowing out from the bottom evaporation passage <NUM> and discharges the fluid to the outside without returning into the bottom liquid storage section <NUM>. The fluid collection section <NUM> is provided with a fluid outlet 13a.

In the multistage liquid storage-type condenser-evaporator disclosed in Patent Document <NUM>, liquid is circulated in all liquid storage sections including the bottom liquid storage section, and an evaporated gas outlet is provided in all circulation liquid storage sections.

On the other hand, in the present embodiment, the bottom liquid storage section <NUM> does not circulate the liquid, so that the evaporated gas cannot be collected. Therefore, the fluid collection section <NUM> independent of the bottom liquid storage section <NUM> is provided in the third evaporation area.

A method of heat exchange between nitrogen gas and oxygen enriched liquid air using the multistage liquid storage-type condenser-evaporator <NUM> having the above configuration will be described together with the operation of the multistage liquid storage-type condenser-evaporator <NUM>.

Oxygen enriched liquid air is supplied from the outside and stored in the top circulation liquid storage section <NUM> via the liquid inlet <NUM>. In the lower liquid storage section, the oxygen enriched liquid air is supplied via the communication passage <NUM>, and stored. In the bottom liquid storage section <NUM>, the oxygen enriched liquid air is supplied via the bottom communication passage <NUM>, and stored.

On the other hand, nitrogen gas is introduced into the condensation passage <NUM> via the nitrogen gas header <NUM>.

The oxygen enriched liquid air stored in the circulation liquid storage section <NUM> flows into the evaporation passage <NUM> by the head pressure, and thereby the liquid level becomes the same in the circulation liquid storage section <NUM> and the evaporation passage <NUM>. Also in bottom liquid storage section <NUM>, the oxygen enriched liquid air is stored, and the liquid level reaches a predetermined height of the evaporation passage <NUM>.

When the nitrogen gas passes through the condensation passage <NUM> in this state, heat is exchanged between the nitrogen gas in the condensation passage <NUM> and the oxygen enriched liquid air in the evaporation passage <NUM>, and a part of the oxygen enriched liquid air evaporates and vaporizes to become evaporated gas. The oxygen enriched liquid air in the evaporation passage <NUM> is in a gas-liquid mixed state (gas-liquid two-phase fluid). Since there is a difference in density between the oxygen enriched liquid air in the gas-liquid mixed state in the evaporation passage <NUM> and the oxygen enriched liquid air in the circulation liquid storage section <NUM>, an ascending flow is generated in the evaporation passage <NUM>, and a gas-liquid two-phase fluid flows out from the evaporation outflow passage 17b. The outflown evaporated gas is led out from the evaporated gas outlet 9a of the circulation liquid storage section <NUM>. The oxygen enriched liquid air which has not evaporated returns into the circulation liquid storage section <NUM>, and a circulating flow is formed between the circulation liquid storage section <NUM> and the evaporation passage <NUM> (thermosiphon action). At this time, the nitrogen concentration of the evaporated gas led out is higher than the nitrogen concentration of the oxygen enriched liquid air supplied from the outside, and is higher than the nitrogen concentration of the circulating flow introduced into the evaporation passage <NUM>.

In the bottom liquid storage section <NUM>, since no circulating flow is generated, the fluid which has ascended in the evaporation passage <NUM> is collected in the fluid collection section <NUM> and discharged to the outside from the fluid outlet 13a.

As described above, since the liquid circulation does not occur in the bottom liquid storage section <NUM>, the nitrogen concentration of the fluid ascending in the evaporation passage <NUM> does not decrease, and the temperature difference between the nitrogen flowing in the condensation passage <NUM> and the oxygen enriched liquid air flowing in the evaporation passage <NUM> can be made larger than that in the conventional condenser-evaporator.

When the liquid level of the circulation liquid storage section <NUM> becomes equal to or higher than the height of the inlet to the communication passage <NUM>, the oxygen enriched liquid air flows into the communication passage <NUM> and is stored in the lower circulation liquid storage section <NUM>.

Similarly, in the bottom circulation liquid storage section <NUM>, when the liquid level exceeds the height of the inlet to the bottom communication passage <NUM>, the oxygen enriched liquid air flows into the bottom communication passage <NUM> and is stored in the bottom liquid storage section <NUM>.

On the other hand, while passing through the condensation passage <NUM>, the nitrogen gas exchanges heat with the oxygen enriched liquid air in the adjacent evaporation passage <NUM>, is condensed (liquefied), descends, and is led out from the lower end of the condensation passage <NUM> through the liquid nitrogen outlet.

In the multistage liquid storage-type condenser-evaporator disclosed in Patent Document <NUM> (Patent No. <NUM>), the liquid circulates between the inlet and the outlet of the evaporation passage <NUM> in all liquid storage sections including the bottom liquid storage section <NUM>.

On the other hand, in the multistage liquid storage-type condenser-evaporator of the present embodiment, the liquid does not flow into the bottom liquid storage section <NUM> from the bottom evaporation passage, that is, the liquid is not circulated. The bottom liquid storage section <NUM> has the same structure as that of the dry-type condenser-evaporator. The oxygen enriched liquid air is supplied into the bottom liquid storage section <NUM> via the bottom communication passage <NUM>, flows into the evaporation inflow passage which is formed at the bottom of the evaporation passage <NUM>, completely evaporates, flows out from the fluid collection section <NUM>, and is led out.

As described above, the oxygen enriched liquid air does not circulate in the bottom liquid storage section <NUM>, so that the nitrogen concentration does not decrease. Therefore, the temperature difference between the nitrogen flowing through the condensation passage <NUM> and the oxygen enriched liquid air can be increased as compared with the case of circulation.

<FIG> is a QT diagram of a multistage liquid storage-type condenser-evaporator having a two-stage evaporation area. Nitrogen gas flows in from the top at the dew point, condenses and flows out from the bottom at the boiling point. Since there is almost no difference between the dew point and the boiling point in nitrogen, the temperature is constant. In the following description, the same parts as those of the three-stage multistage liquid storage-type condenser-evaporator shown in <FIG> are designated by the same reference numerals as those used in <FIG>.

The oxygen enriched liquid air flows into the circulation liquid storage section <NUM> of the first evaporation area at a nitrogen concentration of <NUM>%, flows into the lower part of the evaporation passage <NUM> from the lower part of the circulation liquid storage section <NUM>, ascends due to the slight temperature rise while evaporating, and flows into the circulation liquid storage section <NUM> in the gas-liquid two-phase state. Inflowing gas in the gas-liquid two-phase state is led out from the evaporated gas outlet 9a. Meanwhile, liquid in the gas-liquid two-phase state is returned into the circulation liquid storage section <NUM>. As a result, the nitrogen concentration of the led-out gas (nitrogen enriched gas) increases to <NUM>%, and the nitrogen concentration of the oxygen enriched liquid air in the circulation liquid storage section <NUM> decreases to <NUM>%.

The liquid in the circulation liquid storage section <NUM> is supplied into the bottom liquid storage section <NUM> via the bottom communication passage <NUM>. Then, the liquid flows into the evaporation inflow passage which is formed at the bottom of the evaporation passage <NUM> in the second evaporation area, completely evaporates, and is led out through the fluid collection section <NUM>. Therefore, the nitrogen concentration of the led-out gas (oxygen enriched gas) is equal to the nitrogen concentration of <NUM>% of the oxygen enriched liquid air in circulation liquid storage section <NUM>. Further, the temperature of the evaporation passage <NUM> in the second evaporation area is equal to the oxygen enriched liquid air temperature of the bottom circulation liquid storage section <NUM>, and rises to the dew point with evaporation.

On the other hand, in the conventional condenser-evaporator, as shown in <FIG>, the nitrogen concentration of the oxygen enriched liquid air supplied from the lower part of the evaporation passage <NUM> is reduced to <NUM>% by evaporation and circulation in the second evaporation area. As the boiling point rises, the temperature rises, and the temperature difference between the nitrogen flowing through the condensation passage <NUM> and the oxygen enriched liquid air becomes smaller.

<FIG> is a diagram showing an inflow and an outflow of fluid in the multistage liquid storage-type condenser-evaporator including the circulation liquid storage section <NUM> including an evaporated gas outlet for leading out evaporated gas (GAir: nitrogen enriched gas), a liquid inlet for introducing liquid (LAir: oxygen enriched liquid air) from the outside, and a liquid outlet for leading out (purging) the liquid in the bottom liquid storage section <NUM>.

<FIG> is a diagram showing an inflow and an outflow of fluid in the multistage liquid storage-type condenser-evaporator including a gas-liquid collection container <NUM> which collects the gas which has flowed into the circulation liquid storage section <NUM> and also serves as a bottom liquid storage section <NUM>, and an evaporated gas outlet for leading out evaporated gas (GAir) collected in the gas-liquid collection container <NUM>, wherein the gas-liquid collection container <NUM> includes a liquid outlet for leading out (purging) liquid stored in the gas-liquid collection container <NUM> and a liquid inlet for introducing liquid (LAir) into the circulation liquid storage section <NUM>. In the multistage liquid storage-type condenser-evaporator shown in <FIG>, the evaporation liquid storage section <NUM> is not provided with the evaporated gas outlet 9a. The upper end of the side wall forming the circulation liquid storage section <NUM> is not in contact with the evaporation passage <NUM>. Therefore, the gas from the evaporation passage <NUM> is introduced directly into the gas-liquid collection container <NUM> from the opening of the circulation liquid storage section <NUM>.

The liquid led out through the liquid outlet of the bottom liquid storage section may be depressurized and supplied into the bottom evaporation passage <NUM>.

<FIG> shows a case in which the liquid led out through the liquid outlet of the bottom liquid storage section is depressurized and supplied into the bottom evaporation passage <NUM> in the multistage liquid storage-type condenser-evaporator shown in <FIG>. As shown in <FIG>, a pipe <NUM> connecting between the liquid outlet <NUM> and the inlet of the evaporation passage <NUM> of the bottom evaporation area is provided, and a pressure reducing valve <NUM> is provided in the pipe <NUM>. Further, similarly to the evaporation passage at the first evaporation area, the evaporation passage at the second evaporation area is made by an evaporation inflow passage which is a horizontal fin at the lower part, vertical fins, and an evaporation outflow passage which is a horizontal fin at the upper part.

<FIG> shows a case in which the liquid led out through the liquid outlet of the gas-liquid collection container <NUM> is depressurized and supplied into the bottom evaporation passage <NUM> in the multistage liquid storage-type condenser-evaporator shown in <FIG>. As shown in <FIG>, a pressure reducing valve <NUM> is provided in the pipe <NUM> provided with the liquid outlet of the gas-liquid collection container <NUM>. In <FIG>, the same parts as those in <FIG> are designated by the same reference numerals.

The evaporation region shown in <FIG> has three stages, an odd number of stages. When the evaporation region has four stages, an even number, each passage constituting the heat exchanger core <NUM> is shown in <FIG>. In <FIG>, the same parts as those in <FIG> are designated by the same reference numerals as those in <FIG>.

Next, a nitrogen production device using the multistage liquid storage-type condenser-evaporator <NUM> will be described.

<FIG> shows an embodiment in which the multistage liquid storage-type condenser-evaporator <NUM> is used as a condenser-evaporator of a nitrogen production device which produces nitrogen from air.

The nitrogen production device <NUM> of this embodiment includes a multistage liquid storage-type condenser-evaporator <NUM> including the gas-liquid collection container <NUM> shown in <FIG>.

The nitrogen production device <NUM> of the present embodiment uses at least a part of the gas led out from the fluid collection section <NUM> through the fluid outlet 13a as a cold source, and a part of the gas led out through the opening of the circulation liquid storage section <NUM> and an evaporation gas outlet 9a provided in the gas-liquid collection container <NUM> is used as a raw material for the second distillation column <NUM>.

Hereinafter, the nitrogen production device35 of the present embodiment will be specifically described with reference to <FIG>.

Raw material air is pressurized to a predetermined pressure by the raw material air compressor <NUM>, and then carbon dioxide, water vapor, and trace amounts of other impurities in the raw material air are removed in the pretreatment facility <NUM>.

The raw material air from which impurities have been removed is cooled by a low-temperature gas described later in the main heat exchanger <NUM>, introduced into the distillation column <NUM> by a conduit <NUM> of which a first end (one end) is connected to the raw material air compressor <NUM> and a second end (the other end) is connected to a lower part of the distillation column <NUM>. The raw material air ascends in the distillation column <NUM>, is distilled with a descending liquid described later, the nitrogen component is condensed in the upper part of the distillation column <NUM>, and oxygen enriched liquid air in which the oxygen component is concentrated is collected in the lower part of the distillation column <NUM>.

The nitrogen gas in which the nitrogen component is concentrated is led out from a conduit <NUM> of which a first end is connected to an upper part of the distillation column <NUM>, and a part of the nitrogen gas is introduced through a conduit <NUM> into the main heat exchanger <NUM> to heat exchange with the raw material air, the temperature of the nitrogen gas is raised, and the nitrogen gas is collected as a product nitrogen gas from the conduit <NUM>.

On the other hand, the remaining nitrogen gas in which the nitrogen component is concentrated is introduced into the condensation passage <NUM> of the multistage liquid storage-type condenser-evaporator <NUM> through a conduit <NUM> of which a first end is connected to the conduit <NUM> and a second end is connected to the nitrogen gas introduction pipe 19a provided in the nitrogen gas header <NUM> of the multistage liquid storage-type condenser-evaporator <NUM>. The nitrogen gas is condensed by heat exchange with an oxygen enriched liquid air described later. Then, the condensed liquid nitrogen is introduced into the distillation column <NUM> through a conduit <NUM> of which a first end is connected to the liquid outlet <NUM> and a second end is connected to the upper part of the distillation column <NUM>, and becomes the descending liquid in the distillation column <NUM>.

Most of the oxygen enriched liquid air in the lower part of the first distillation column <NUM> is led out into a conduit <NUM> of which a first end is connected to the bottom of the distillation column <NUM> and a second end is connected to a pressure reducing valve <NUM>, and depressurized by the pressure reducing valve <NUM>. Then, the depressurized oxygen enriched liquid air is introduced into the multistage liquid storage-type condenser-evaporator <NUM> through a conduit <NUM> of which a first end is connected to the pressure reducing valve <NUM> and a second end is connected to the liquid inlet <NUM> of the multistage liquid storage-type condenser-evaporator <NUM>. The oxygen enriched liquid air introduced into the multistage liquid storage-type condenser-evaporator <NUM> is vaporized by heat exchange with the nitrogen gas described above. Then, a part of the evaporated gas, that is, the gas having a low nitrogen concentration, which flows in the bottom evaporation passage <NUM> and is collected in the fluid collection section <NUM> is led out as waste gas for a cold source by a conduit <NUM>, of which a first end is connected to the fluid outlet 13a of the fluid collection section <NUM> and a second end is connected to an expansion turbine <NUM>, is heated by the main heat exchanger <NUM>, and introduced into the expansion turbine <NUM>.

The waste gas which has generated cold required for the device in the expansion turbine <NUM> is introduced into the main heat exchanger <NUM> by a conduit <NUM>, cools the raw material air, and reaches room temperature.

Components other than liquid contained in the oxygen enriched liquid air introduced in the multistage liquid storage-type condenser-evaporator <NUM>, that is, evaporated gas led out from the opening of circulation liquid storage section <NUM>, is once introduced into the gas-liquid collection container <NUM>, led out through the conduit <NUM>, of which a first end is connected to the evaporated gas outlet 9a provided at the upper part of the gas-liquid collection container <NUM> and a second end is connected to the lower part of the second distillation column <NUM>, as an exhaust gas for improving the nitrogen recovery rate having a high nitrogen concentration, and introduced into the lower part of the second distillation column <NUM> as a raw material gas.

The gas introduced into the lower part of the second distillation column <NUM> ascends in the second distillation column <NUM>, by distillation with the descending liquid described later, the nitrogen component is concentrated in the upper part of the second distillation column <NUM> and the oxygen enriched liquid air in which oxygen components are concentrated is collected in the lower part of the second distillation column <NUM>.

The nitrogen gas in which the nitrogen component is concentrated is led out through a conduit <NUM> of which a first end is connected to the upper part of the second distillation column <NUM> and a second end is connected to a conduit <NUM> described later. A portion of the nitrogen gas is then introduced into the main heat exchanger <NUM> via the conduit <NUM>. Therefore, the temperature of the nitrogen gas is raised by heat exchange with the raw material air, and the nitrogen gas is collected from a conduit <NUM> as a second product nitrogen gas.

On the other hand, the remaining nitrogen gas with concentrated nitrogen components led out through the conduit <NUM> is introduced into the condenser-evaporator <NUM> via a conduit <NUM> branched from the conduit <NUM>, and condensed by heat exchange with oxygen enriched liquid air described later. Next, the condensed nitrogen gas is introduced into the second distillation column <NUM> through a conduit <NUM> of which a first end is connected to the condenser-evaporator <NUM> and a second end is connected to the upper part of the second distillation column <NUM>, and becomes a descending liquid.

The oxygen enriched liquid air in the lower part of the second distillation column <NUM> is led out into a conduit <NUM> of which a first end is connected to the bottom of the second distillation column <NUM> and a second end is connected to the pressure reducing valve <NUM>, and then the pressure thereof is reduced by the pressure reducing valve <NUM>. The oxygen enriched liquid air is then introduced into the condenser-evaporator <NUM> through a conduit <NUM> of which a first end is connected to the pressure reducing valve <NUM> and a second end is connected to the condenser-evaporator <NUM>. The oxygen enriched liquid air introduced into the condenser-evaporator <NUM> is vaporized by heat exchange with the nitrogen gas described above, and then joins the waste gas from the expansion turbine <NUM> described above through a conduit <NUM>.

As a part of the cold required for the second distillation column <NUM>, a part of the oxygen enriched liquid air which is led out through a conduit <NUM> of which a first end is connected to the bottom of the distillation column <NUM> is used.

In this embodiment, a part of the oxygen enriched liquid air in the lower part of the distillation column <NUM> becomes an exhaust gas containing a large amount of nitrogen compositions by the multistage liquid storage-type condenser-evaporator <NUM>, and is supplied as a raw material gas for the second distillation column <NUM>. Therefore, the nitrogen recovery rate of the second distillation column <NUM> is improved.

Hereinafter, a nitrogen production device of a second embodiment will be specifically described with reference to <FIG>. In <FIG>, the same parts as those in <FIG> are designated by the same reference numerals.

The nitrogen production device <NUM> of the present embodiment includes a multistage liquid storage-type condenser-evaporator including the gas-liquid collection device <NUM> shown in <FIG>.

The nitrogen production device <NUM> of the present embodiment uses at least a part of the gas led out from the fluid collection section <NUM> through the opening of the circulation liquid storage section <NUM> and an evaporation gas outlet 9a provided in the gas-liquid collection container <NUM> as a part of the raw material air.

Raw material air is pressurized to a predetermined pressure by the raw material air compressor <NUM>, and then carbon dioxide, water vapor, and trace amounts of other impurities in the raw material air are removed in the pretreatment facility <NUM>. The raw material air from which impurities have been removed is cooled by a low-temperature gas described later in the main heat exchanger <NUM>, and introduced into the distillation column <NUM> by the conduit <NUM> of which the first end (one end) is connected to the raw material air compressor <NUM> and the second end (the other end) is connected to the lower part of the distillation column <NUM>. The raw material air ascends in the distillation column <NUM>, is distilled with a descending liquid described later, the nitrogen component is condensed in the upper part of the distillation column <NUM>, and oxygen enriched liquid air in which the oxygen component is concentrated is collected in the lower part of the distillation column <NUM>.

The nitrogen gas in which the nitrogen component is concentrated is led out from the conduit <NUM> of which the first end is connected to an upper part of the distillation column <NUM>, a part of the nitrogen gas is introduced through the conduit <NUM> into the main heat exchanger <NUM> to heat exchange with the raw material air, the temperature of the nitrogen gas is raised, and the nitrogen gas is collected as a product nitrogen gas from the conduit <NUM>.

On the other hand, the remaining nitrogen gas in which the nitrogen component is concentrated is introduced into the condensation passage <NUM> of the multistage liquid storage-type condenser-evaporator <NUM> through the conduit <NUM> of which the first end is connected to the conduit <NUM> and the second end is connected to the nitrogen gas introduction pipe 19a provided in the nitrogen gas header <NUM> of the multistage liquid storage-type condenser-evaporator <NUM>. The nitrogen gas is condensed by heat exchange with an oxygen enriched liquid air described later. Then, the condensed liquid nitrogen is introduced into the distillation column <NUM> through the conduit <NUM> of which the first end is connected to the liquid outlet <NUM> and the second end is connected to the upper part of the distillation column <NUM>, and becomes the descending liquid in the distillation column <NUM>.

The oxygen enriched liquid air in the lower part of the distillation column <NUM> is led out into the conduit <NUM> of which the first end is connected to the bottom of the distillation column <NUM> and the second end is connected to the pressure reducing valve <NUM>, and depressurized by the pressure reducing valve <NUM>. Then, the depressurized oxygen enriched liquid air is introduced into the multistage liquid storage-type condenser-evaporator <NUM> through the conduit <NUM>, of which a first end is connected to the pressure reducing valve <NUM> and the second end is connected to the liquid inlet <NUM> of the multistage liquid storage-type condenser-evaporator <NUM>, and the opening of the circulation liquid storage section <NUM>. A part of the oxygen enriched liquid air introduced into the multistage liquid storage-type condenser-evaporator <NUM> is evaporated in the top evaporation passage <NUM> by heat exchange with the nitrogen gas described above. The oxygen enriched liquid air which has not evaporated is stored in the gas-liquid collection container <NUM> which also serves as the bottom liquid storage section <NUM> through the bottom communication passage <NUM>. The stored oxygen enriched liquid air passes through a conduit provided at the bottom of the gas-liquid collection container <NUM>, is decompressed by a pressure reducing valve <NUM>, supplied into the bottom evaporation passage <NUM>, and is completely vaporized. Then, the vaporized oxygen enriched air is then led out as waste gas for a cold source with a low nitrogen concentration through the fluid collection section <NUM> and the conduit <NUM> of which the first end is connected to the fluid outlet 13a and the second end is connected to the expansion turbine <NUM>. The led-out waste gas is heated in the main heat exchanger <NUM>, introduced into the expansion turbine <NUM> to generate cold required for the device, introduced into the main heat exchanger <NUM> by the conduit <NUM>, cools the raw material air, and reaches room temperature.

Components other than liquid contained in the oxygen enriched liquid air introduced into the multistage liquid storage-type condenser-evaporator <NUM>, that is, the gas led out from the opening of the circulation liquid storage section <NUM> is led out through a conduit <NUM>, of which a first end is connected to the evaporated gas outlet 9a provided on the upper part of the gas-liquid collection container <NUM>, as an exhaust gas for improving the nitrogen recovery rate, which has a large nitrogen composition, is pressurized by a expansion turbine blower <NUM>, introduced into the raw material air, and becomes a part of the raw material gas of the distillation column <NUM>.

Claim 1:
A multistage liquid storage-type condenser-evaporator (<NUM>) comprising:
a condensation passage (<NUM>) which is configured to communicate in a vertical direction in which gas flows and is condensed;
an evaporation passage (<NUM>) which is configured to be divided into multiple stages in a vertical direction, through which liquid which is evaporated by exchanging heat with the gas flows;
circulation liquid storage sections (<NUM>) which are configured to be provided corresponding to the evaporation passage (<NUM>) at each stage except a bottom stage, supply the liquid into the evaporation passage (<NUM>), store the liquid flowing out from the evaporation passage (<NUM>), and circulate the liquid in the evaporation passage (<NUM>) at each stage;
a communication passage (<NUM>) which is configured to flow the liquid in the circulation liquid storage section (<NUM>) at an upper stage into the circulation liquid storage section (<NUM>) at lower stage; and
a bottom communication passage (<NUM>) which is configured to flow liquid in a bottom circulation liquid storage section into a bottom liquid storage section (<NUM>),
the condensation passage (<NUM>) and the evaporation passage (<NUM>) are stacked to form a heat exchange section (<NUM>),
the heat exchange section (<NUM>) forms the heat exchanger core (<NUM>), and
the circulation liquid storage section (<NUM>) is formed on at least one side surface in a width direction of the heat exchanger core (<NUM>) orthogonal to the stacking direction, corresponding to the number of stages of the evaporation passage (<NUM>),
wherein the multistage liquid storage-type condenser-evaporator (<NUM>) further comprises:
the bottom liquid storage section (<NUM>) which is configured to store the liquid supplied into the bottom evaporation passage without circulating, and
a fluid collection section (<NUM>) which is configured to collect the fluid which flows out from the bottom evaporation passage and discharge to the outside without returning into the bottom liquid storage section (<NUM>).