JP2017161199A - Cold water manufacturing system - Google Patents

Abstract

PROBLEM TO BE SOLVED: To inexpensively manufacture cold water by water self-sustenance of a fuel cell unit and an adsorption type refrigerating machine, in a cold water manufacturing system composed of the fuel cell unit and the adsorption type refrigerating machine.SOLUTION: A cold water manufacturing device includes: a fuel cell unit 2; an adsorption type refrigerating machine 5 including an adsorber/desorber 51, an evaporator 52 and a refrigerant condenser 53; a first heat exchanger 3 exchanging heat between heating fluid W2 and an off-gas G1; an off-gas condenser 4 producing condensate W1 by cooling the off-gas G1; a cooling unit 6 for cooling cooling fluid W3; a first branched cooling fluid line L91 branched from a cooling fluid line L7 and joined with the cooling fluid line L7 again through the off-gas condenser 4; first flow rate adjustment means V11 for adjusting a flow rate of cooling fluid W31 circulated in the first branched cooling fluid line L91; and a control portion 10 for controlling the first flow rate adjustment means V11 so that a temperature of an off-gas G2 measured by first temperature measurement means S1 becomes lower than a first set temperature.SELECTED DRAWING: Figure 1

Description

  The present invention relates to a cold water production system including a fuel cell unit and an adsorption refrigerator that produces cold water from supply water.

  2. Description of the Related Art Conventionally, there is known a combined fuel cell system including a fuel cell unit and an adsorption refrigerator having an adsorption / desorption device, an evaporator, and a refrigerant condenser (see, for example, Patent Document 1). In the hybrid fuel cell system described in Patent Document 1, the adsorption / desorption device can be switched between an adsorption process in which the refrigerant vapor is adsorbed on the adsorbent by cold heat and a desorption process in which the refrigerant vapor is desorbed from the adsorbent by heat. It is. In addition, the adsorption refrigerator can produce cold water of 10 ° C. or lower if, for example, room temperature water is used as a cooling target fluid to be circulated through the evaporator.

In the combined fuel cell system described in Patent Document 1, the adsorption / desorption device of the adsorption refrigeration unit, for example, uses the heat of hot water (heating fluid) obtained by heat exchange with off-gas discharged from the fuel cell unit. Used in the desorption process. The adsorption / desorption device of the adsorption refrigerator uses, for example, the cold heat of cooling water (cooling fluid) in the adsorption process.
In recent years, an adsorption refrigeration machine that uses an adsorbent capable of performing a desorption process with a low temperature of about 60 to 75 ° C. has appeared on the market, and the use of this adsorption refrigeration machine in combination with a fuel cell unit has also been studied. Yes. Specifically, there is a case where hot water obtained by heat exchange with off-gas discharged from the fuel cell unit is used as a heat source during the desorption process of the adsorption / desorption device of the adsorption refrigerator. Since the temperature of the off gas during power generation reaches about 300 ° C., hot water of 75 ° C. or less can be easily obtained by heat exchange.

  A fuel cell system including a fuel cell unit and a refrigerator is known (see, for example, Patent Document 2). In the fuel cell unit, power is generated by a reaction between a reformed gas containing hydrogen (reformed fuel gas) and oxygen in the air (oxidant gas). The fuel cell system described in Patent Document 2 is a so-called “water self-sustained” in which off-gas is cooled to generate condensed water without requiring supply of water from the outside and reused when generating reformed gas. Is realized. Water independence is a useful technology in the field of fuel cells because it can continue power generation even when water outages occur during power outages or disasters. In the fuel cell system in which water is supplied by water self-supporting described in Patent Document 2, the off-gas discharged from the fuel cell is cooled using cooling water produced by a refrigerator to generate condensed water.

Japanese Patent No. 5625368 JP 2009-170189 A

In the composite fuel cell system described in Patent Document 1, if water self-supporting in Patent Document 2 is realized, it is possible to always generate power without being affected by water interruption or the like, so that it is expected to further contribute to energy saving. However, in the technique described in Patent Document 2, since the refrigerator that supplies the cooling water has a structure that consumes a large amount of electric power, power is directly supplied from the fuel cell unit to the refrigerator, or an inexpensive external device is used. If the nighttime power is not used, the running cost of the entire system tends to be high.
On the other hand, in the fuel cell unit to which water is supplied by water self-supporting, when the off-gas discharged from the fuel cell unit cannot be sufficiently cooled, the amount of condensed water necessary for generating reformed gas (fuel gas) May not be generated.

  The present invention provides a cold water production system comprising a fuel cell unit and an adsorption refrigeration machine, and reliably produces an amount of condensed water necessary for the water self-supporting of the fuel cell unit, while producing an inexpensive chilled water with an adsorption refrigeration machine. It aims to be realized.

  The present invention includes a fuel cell unit that introduces a fuel gas and an oxidant gas into a battery stack and generates power by an electrochemical reaction, an adsorption process in which refrigerant vapor is adsorbed to an adsorbent by cold heat, and refrigerant vapor from the adsorbent by hot heat. An adsorption / desorption device that can be switched between desorption processes to be desorbed, an evaporator that vaporizes the refrigerant liquid as the refrigerant vapor is adsorbed on the adsorbent, and a refrigerant vapor that is condensed when the refrigerant vapor is desorbed from the adsorbent. A refrigerant condenser, a cooling fluid line in which a cooling fluid for supplying cold to the adsorbent in the adsorption process circulates, and a heating fluid for applying warm heat to the adsorbent in the desorption process Is connected to a heating fluid line through which the circulating water circulates, and a supply water line through which the supply water circulates is connected to the evaporator, and the refrigerant liquid is vaporized in the evaporator. An adsorption refrigerator that produces cold water from supply water by heat of vaporization, an offgas line through which offgas discharged from the fuel cell unit flows, a heating fluid that flows through the heating fluid line, and an offgas that flows through the offgas line A first heat exchanger for exchanging heat between, an off-gas condenser that circulates through the off-gas line and cools off-gas after heat exchange in the first heat exchanger to generate condensed water, and A cooling unit that cools the cooling fluid circulating through the cooling fluid line, a first branch cooling fluid line that branches off from the cooling fluid line and rejoins the cooling fluid line via the off-gas condenser, A first flow rate adjusting means for adjusting the flow rate of the cooling fluid flowing through the first branch cooling fluid line, and the off-gas line downstream from the off-gas condenser. A first temperature measuring means for measuring the temperature of the off-gas, and a controller for controlling the first flow rate adjusting means so that the temperature of the off-gas measured by the first temperature measuring means is lower than the first set temperature. The present invention relates to a cold water production system.

  Also, heating that branches from the heating fluid line upstream of the first heat exchanger, bypasses the first heat exchanger, and rejoins the heating fluid line downstream of the first heat exchanger. A fluid bypass line, a second flow rate adjusting means for adjusting a flow rate of the heated fluid flowing through the heated fluid bypass line, and a second temperature measuring means for measuring the temperature of the heated fluid supplied to the adsorption / desorption device. In addition, it is preferable that the control unit controls the second flow rate adjusting unit so as to maintain the temperature of the heated fluid measured by the second temperature measuring unit in a second set temperature range.

  The control system further comprises a circulation pump provided in the heating fluid line, the rotation speed of which can be adjusted by an inverter, and a second temperature measurement means for measuring the temperature of the heating fluid supplied to the adsorption / desorption device. Preferably, the unit controls the rotational speed of the circulation pump via the inverter so as to maintain the temperature of the heated fluid measured by the second temperature measuring means in a second set temperature range.

  A second branch cooling fluid line branched from the cooling fluid line and rejoining the cooling fluid line; a heating fluid flowing through the heating fluid line upstream of the adsorption / desorption device; and the second branch cooling. A second heat exchanger for exchanging heat with the cooling fluid flowing through the fluid line, a third flow rate adjusting means for adjusting the flow rate of the cooling fluid flowing through the second branch cooling fluid line, and the adsorption / desorption device And a second temperature measuring means for measuring the temperature of the heated fluid supplied to the controller, wherein the control unit maintains the temperature of the heated fluid measured by the second temperature measuring means in a second set temperature range. It is preferable to control the third flow rate adjusting means.

  A branch from the off-gas line upstream of the first heat exchanger, bypassing the first heat exchanger, downstream of the first heat exchanger and upstream of the off-gas condenser; An off-gas bypass line that rejoins the off-gas line; a fourth flow rate adjusting means that adjusts a flow rate of the off-gas flowing through the off-gas bypass line; and a second temperature that measures the temperature of the heating fluid supplied to the adsorption / desorption device. Measuring means, and the control unit preferably controls the fourth flow rate adjusting means so as to maintain the temperature of the heated fluid measured by the second temperature measuring means within a second set temperature range. .

  According to the present invention, in a chilled water production system comprising a fuel cell unit and an adsorption chiller, an inexpensive chilled water produced by an adsorption chiller can be produced while reliably generating the amount of condensed water necessary for water self-supporting of the fuel cell unit. Manufacturing can be realized.

It is the whole flowchart which shows one Embodiment of the cold water manufacturing system 1 of this invention. 1 is a flowchart showing an embodiment of a cold water production system 1 according to the present invention, and is a diagram showing a main configuration around a fuel cell unit 2. FIG. It is a figure which shows the main structures of the periphery of the adsorption-type refrigerator 5, Comprising: It is a figure which shows the case where an adsorption process is performed in the 1st adsorption / desorption device 51a, and a desorption process is performed in the 2nd adsorption / desorption device 51b. . It is a figure which shows the main structures of the periphery of adsorption | suction type refrigerator 5, Comprising: It is a figure which shows the case where the desorption process is performed in the 1st adsorption / desorption device 51a, and the adsorption process is performed in the 2nd adsorption / desorption device 51b. . It is a flowchart explaining the 1st structural example changed from the structure shown in FIG. It is a flowchart explaining the 2nd structural example changed from the structure shown in FIG. It is a flowchart explaining the 3rd structural example changed from the structure shown in FIG. It is a flowchart explaining the 4th structural example changed from the structure shown in FIG.

  An embodiment of the cold water production system of the present invention will be described with reference to the drawings. FIG. 1 is an overall flowchart showing an embodiment of the cold water production system 1 of the present invention. FIG. 2 is a flowchart showing an embodiment of the cold water production system 1 of the present invention, and is a diagram showing a main configuration around the fuel cell unit 2. FIG. 3 is a diagram showing a main configuration around the adsorption refrigerator 5, in which the adsorption process is performed in the first adsorption / desorption device 51a and the desorption process is performed in the second adsorption / desorption device 51b. FIG. FIG. 4 is a diagram showing a main configuration around the adsorption refrigerator 5, and shows a case where the desorption process is executed in the first adsorption / desorption device 51a and the adsorption process is executed in the second adsorption / desorption device 51b. FIG.

As shown in FIG. 1, the cold water production system 1 of the present embodiment collects condensed water from the off gas of the fuel cell unit to perform water self-sustained operation of the fuel cell unit and collects waste heat from the off gas of the fuel cell unit. Thus, it is used as a driving heat source for the adsorption refrigerator. The cold water production system 1 includes a fuel cell unit 2, a first heat exchanger 3, an off-gas condenser 4, an adsorption refrigeration machine 5, a reforming water tank 41, a cooling tower 6 as a cooling unit, an adsorption A flow path switching control valve 7 capable of switching the flow path to which the refrigeration machine 5 is connected, a facility 11 for using cold water, a first proportional control three-way valve V11 as a first flow rate adjusting means, and a first temperature measuring means First temperature sensor S1.
As shown in FIG. 1, the cold water production system 1 includes an off-gas line L1, a condensed water delivery line L21, a reformed water supply line L22, and a heating fluid line L6 (L61, L51, L62) as lines. The cooling fluid line L7 (L71, L51, L72), the first branch cooling fluid line L91, and the cold water production line L100 (L101, L102, L103) are provided. “Line” is a general term for lines capable of flowing fluid such as flow paths, paths, and pipelines.

In addition to the configuration shown in FIG. 1, the cold water production system 1 includes a circulation pump 31, an inverter 32, a second heat exchanger 8, a refrigerant liquid pump 56, as shown in FIGS. 2 to 4. A second proportional control three-way valve V12 as a second flow rate adjustment means, a third proportional control three-way valve V13 as a third flow rate adjustment means, a fourth proportional control three-way valve V14 as a fourth flow rate adjustment means, Second temperature sensors S2a and S2b as temperature measuring means and a control unit 10 are provided. The control unit 10 is connected to each device by a signal line (not shown) so as to be able to control each device to be controlled.
2 to 4, in addition to the configuration shown in FIG. 1, the cold water production system 1 includes, as lines, a fuel supply line L31, an air supply line L32, a reformed gas supply line L33, An off-gas bypass line L4, a heating fluid bypass line L8, and a second branch cooling fluid line L92 are provided.

As shown in FIG. 2, the fuel cell unit 2 includes a battery stack 20 and a reformer 21. The fuel cell unit 2 introduces a reformed gas G4 containing hydrogen (reformed fuel gas) and air A1 (oxidant gas) into the battery stack 20. The reformed gas G4 is generated in the reformer 21 by reacting the raw fuel gas G3 and the steam of the reformed water W1. The fuel cell unit 2 generates power by an electrochemical reaction between the reformed gas G4 containing hydrogen and oxygen (oxidant gas) in the air A1. The battery stack 20 is configured by stacking solid oxide fuel cells (SOFC) cells. The operating temperature, which is the temperature when power generation is performed in the battery stack 20, is as high as 700 ° C to 1000 ° C. The electricity generated by the battery stack 20 is sent to a power conditioner (not shown) and converted into an AC voltage.
Further, the fuel cell unit 2 discharges the off gas G1. The temperature of the off gas G1 discharged from the fuel cell unit 2 is about 300 ° C. The off gas G1 discharged from the fuel cell unit 2 is relatively small.

  The reformed gas supply line L <b> 33 causes the reformed gas G <b> 4 containing hydrogen generated in the reformer 21 to flow toward the battery stack 20. An upstream end portion of the reformed gas supply line L33 is connected to the reformer 21, and a downstream end portion of the reformed gas supply line L33 is connected to the battery stack 20.

  A catalyst is accommodated in the reformer 21. The reformer 21 causes the reformed water W1 supplied through the reformed water supply line L22 (described later) and the raw fuel gas G3 supplied through the fuel supply line L31 to react on the catalyst (steam reforming method). ). By this reaction, the reformed gas G4 is generated in the reformer 21. The generated reformed gas G4 is supplied to the battery stack 20 through the reformed gas supply line L33.

  The fuel supply line L31 distributes the raw fuel gas G3 from the fuel supply unit (not shown) to the reformer 21. The upstream end of the fuel supply line L31 is connected to a fuel supply unit (not shown) capable of supplying raw fuel gas G3 such as city gas, and the downstream end of the fuel supply line L31 is The reformer 21 is connected.

  The air supply line L32 distributes the air A1 that has passed through a blower (not shown) and a filter (not shown) to the battery stack 20. The upstream end of the air supply line L32 is connected to a blower (not shown) and a filter (not shown) for supplying the air A1 to the fuel cell unit 2. The downstream end of the air supply line L32 is connected to the battery stack 20.

The off gas line L1 is a line through which the off gas G1 discharged from the fuel cell unit 2 flows. The off gas line L1 includes a first off gas line L11, a second off gas line L12, and a third off gas line L13.
The upstream end portion of the first off-gas line L11 is connected to the battery stack 20. The downstream end of the first off-gas line L11 is connected to the first heat exchanger 3. A fourth proportional control three-way valve V14 is disposed in the first off gas line L11.

  From the middle of the first off-gas line L11, the off-gas bypass line L4 branches off at the fourth proportional control three-way valve V14. The downstream end of the off-gas bypass line L4 is connected to the connection portion J11 of the second off-gas line L12. The off gas bypass line L4 branches from the first off gas line L11 on the upstream side of the first heat exchanger 3 at the fourth proportional control three-way valve V14, bypasses the first heat exchanger 3, and passes through the second off gas line L12. In the connection part J11, it merges again in the 2nd off-gas line L12 in the downstream of the 1st heat exchanger 3, and the upstream of the off-gas condenser 4. FIG.

  The fourth proportional control three-way valve V14 is provided at a portion of the first offgas line L11 that branches to the offgas bypass line L4. The fourth proportional control three-way valve V14 is configured by a motor valve, and is a valve capable of adjusting the flow rate of the offgas G12 flowing through the offgas bypass line L4 by adjusting the valve opening degree. That is, the fourth proportional control three-way valve V14 is a valve that can change the flow rate ratio of the offgas G12 that is branched from the first offgas line L11 to the offgas bypass line L4. In addition, the ratio of the flow rate of the off gas G12 distributed by the fourth proportional control three-way valve V14 is 0 (zero) in the ratio of the flow rate of the off gas G12 that is divided into either the first off gas line L11 or the off gas bypass line L4. May be. The flow rate of the off gas G12 adjusted by the fourth proportional control three-way valve V14 is controlled by a flow rate adjustment signal from the control unit 10.

  The first heat exchanger 3 exchanges heat between a heating fluid W2 that flows through a heating fluid line L6, which will be described later, and an offgas G1 that is discharged from the fuel cell unit 2 and flows through the offgas line L1. That is, the first heat exchanger 3 transmits the waste heat of the off gas G1 discharged from the fuel cell unit 2 to the heating fluid W2 that flows through the heating fluid line L6. The temperature of the off-gas G1 discharged from the fuel cell unit is about 300 ° C., and the temperature of the heating fluid W2 generated by the heat exchange of the first heat exchanger 3 is in the regeneration temperature zone of the adsorbent K described later. Although it depends, it is about 50-100 degreeC.

  The second off gas line L12 is a line from the first heat exchanger 3 to the off gas condenser 4. The upstream end of the second off-gas line L12 is connected to the first heat exchanger 3. The downstream end of the second offgas line L12 is connected to the offgas condenser 4. A connection portion J11 is provided in the second off gas line L12. The downstream end of the aforementioned off-gas bypass line L4 is connected to the connecting part J11.

  The off-gas condenser 4 circulates through the off-gas line L1 and cools off-gas G1 after heat exchange in the first heat exchanger 3 to generate condensed water W1 and water self-supporting (that is, reforming of condensed water W1). The off-gas G2 cooled to a temperature at which reuse as the quality water W1 can be achieved is generated. A first branch cooling fluid line L91 (described later) through which the cooling fluid W31 passes is passed through the off-gas condenser 4. The off-gas condenser 4 cools the off-gas G1 after flowing through the off-gas line L1 and heat-exchanged by the first heat exchanger 3 with the cooling fluid W31 flowing through the first branch cooling fluid line L91, thereby condensing water W1. Is generated.

  The off gas G2 generated by the off gas condenser 4 and the condensed water W1 flow through the third off gas line L13. The upstream end of the third offgas line L13 is connected to the offgas condenser 4. The downstream end of the third off gas line L13 is open to the atmosphere. The third off gas line L13 is provided with a connection portion J12. An upstream end portion of a condensed water delivery line L21 described later is connected to the connection portion J12. The offgas G2 and the condensed water W1 discharged from the offgas condenser 4 are separated at the connection portion J12, and the offgas G2 flows through the third offgas line L13, while the condensed water W1 flows into the condensed water delivery line L21. Circulate. The third off-gas line L13 located on the downstream side of the connection portion J12 discharges the off-gas G2 out of the system.

  A first temperature sensor S1 is provided in the third off-gas line L13 located on the downstream side of the connection portion J12. The first temperature sensor S <b> 1 measures the temperature of the offgas G <b> 2 flowing through the third offgas line L <b> 13 on the downstream side of the offgas condenser 4. The temperature of the off gas G2 measured by the first temperature sensor S1 is transmitted to the control unit 10 as a detection signal.

The condensed water delivery line L <b> 21 circulates the condensed water W <b> 1 generated by the off-gas condenser 4 and separated at the connection portion J <b> 12 toward the reforming water tank 41. The reformed water tank 41 stores the condensed water W1 generated by the off-gas condenser 4 as reformed water.
The reforming water supply line L22 distributes the reforming water W1 (condensed water) stored in the reforming water tank 41 toward the reformer 21. The upstream end of the reforming water supply line L22 is connected to the reforming water tank 41. The downstream end of the reforming water supply line L22 is connected to the reformer 21.

The adsorption refrigerator 5 produces cold water W11 from the supply water W10.
As shown in FIGS. 3 and 4, the adsorption refrigerator 5 includes a refrigerator main body 50, a first adsorption / desorption device 51a, a second adsorption / desorption device 51b, an evaporator 52, a refrigerant condenser 53, Is provided. The first adsorption / desorption device 51 a, the second adsorption / desorption device 51 b, the evaporator 52, and the refrigerant condenser 53 are partitioned inside the refrigerator main body 50. The inside of the refrigerator main body 50 is depressurized to a vacuum state.

  The first adsorption / desorption device 51a and the second adsorption / desorption device 51b are arranged side by side in a substantially horizontal direction. The evaporator 52 is disposed below the first adsorption / desorption device 51a and the second adsorption / desorption device 51b. The refrigerant condenser 53 is disposed above the first adsorption / desorption device 51a and the second adsorption / desorption device 51b. The first adsorption / desorption device 51a and the second adsorption / desorption device 51b have different timings for performing an adsorption process or a desorption process described later. However, the first adsorption / desorption device 51a and the second adsorption / desorption device 51b have the same function when executing the adsorption process, and the same function when executing the desorption process. When it is not necessary to distinguish the first adsorption / desorption device 51a and the second adsorption / desorption device 51b, they are simply referred to as “adsorption / desorption device 51”.

An evaporator-side on-off valve body 54a for opening and closing the communication path is disposed in the communication path where the first adsorption / desorption device 51a and the evaporator 52 communicate with each other. An evaporator side on-off valve body 54b for opening and closing the communication path is disposed in the communication path where the second adsorption / desorption device 51b and the evaporator 52 communicate with each other. When the evaporator side opening / closing valve bodies 54a and 54b are controlled by the control unit 10 so as to be opened when the adsorption / desorption devices 51a and 51b perform the adsorption process, respectively, Are controlled by the control unit 10 so as to be in a closed state.
The evaporator-side on-off valve bodies 54a and 54b allow the refrigerant vapor to flow from the evaporator 52 to the adsorption / desorption devices 51a and 51b in the open state, respectively, and from the adsorption / desorption devices 51a and 51b to the evaporator 52, respectively. It functions as a check valve that does not allow refrigerant vapor to flow.

A refrigerant condenser side opening / closing valve body 55a for opening and closing the communication path is disposed in the communication path where the first adsorption / desorption device 51a and the refrigerant condenser 53 communicate with each other. A refrigerant condenser side opening / closing valve body 55b for opening and closing the communication path is disposed in the communication path where the second adsorption / desorption device 51b and the refrigerant condenser 53 communicate with each other. The refrigerant condenser side opening / closing valve bodies 55a and 55b are controlled by the control unit 10 so as to be closed when the adsorption / desorption devices 51a and 51b perform the adsorption process, and execute the desorption process. In such a case, the control unit 10 controls so as to be in the open state.
The refrigerant condenser side opening / closing valve bodies 55a and 55b allow the refrigerant vapor to flow from the respective adsorption / desorption devices 51a and 51b to the refrigerant condenser 53 in the open state, and the refrigerant condenser 53 to each adsorption / desorption device 51a. , 51b functions as a check valve that does not allow refrigerant vapor to flow to 51b.

Each adsorption / desorption device 51 has an adsorbent K therein. Examples of the adsorbent K include a water vapor adsorbent made of zeolite containing aluminum, phosphorus, and iron in a skeleton structure. This water vapor adsorbent has the characteristic of drawing an adsorption isotherm that increases the amount of water vapor (refrigerant vapor) adsorbed within a narrow relative vapor pressure range, and is sold under the trade name "AQSOA" by Mitsubishi Plastics. What is being done can be illustrated. The regeneration temperature zone of this water vapor adsorbent (the temperature range in which refrigerant vapor desorption occurs) depends on the relative vapor pressure of the portion where the adsorption isotherm starts to rise. The relative vapor pressure is the vapor pressure obtained by dividing the water vapor pressure around the adsorbent by the water vapor saturation pressure at the adsorbent temperature, and the adsorption amount is the amount of water that can be adsorbed by the adsorbent per 1 kg of dry weight. kg.
The first adsorption / desorption device 51a and the second adsorption / desorption device 51b can be switched between an adsorption process in which the refrigerant vapor is adsorbed on the adsorbent K by cold heat and a desorption process in which the refrigerant vapor is desorbed from the adsorbent K by heat. It is.

  The adsorbent K adsorbs the refrigerant vapor by the cold heat of the cooling fluid W3 in the adsorption process, and desorbs the refrigerant vapor (releases water vapor) by the heat of the heating fluid W2 in the desorption process. If the heating fluid W2 is too hot, the adsorbent K may be destroyed. For this reason, the temperature of the heating fluid W2 is preferably lower than a predetermined temperature. For example, the temperature of the heating fluid W2 is preferably maintained in the second set temperature range as the temperature of the heating fluid W2 measured by second temperature sensors S2a and S2b described later.

  The first adsorption / desorption device 51a and the second adsorption / desorption device 51b are connected to a cooling fluid line L7 (cooling / heating supply lines L51 (L51a, L51b)) in the adsorption process, and in the desorption process, the heating fluid line. L6 (cooling / heating supply line L51 (L51a, L51b)) is connected.

  A part of a cold / hot heat supply line L51 (L51a, L51b) for cooling or heating the adsorbent K is disposed inside each of the first adsorption / desorption device 51a and the second adsorption / desorption device 51b. The cold / hot heat supply line L51 (L51a, L51b) connected to the first adsorption / desorption device 51a and the second adsorption / desorption device 51b is one of the cooling fluid lines L7 by switching the flow path of the flow path switching control valve 7 described later. It switches so that a part (refer FIG. 3, FIG. 4) or some heating fluid line L6 (refer FIG. 3, FIG. 4) may be comprised.

  As shown in FIGS. 3 and 4, the flow path switching control valve 7 includes an introduction side switching valve 71 and a derivation side switching valve 72. The introduction side switching valve 71 switches the fluid introduced into the first adsorption / desorption device 51a or the second adsorption / desorption device 51b to the heating fluid W2 or the cooling fluid W3. The derivation side switching valve 72 switches the fluid derived from the first adsorption / desorption device 51a or the second adsorption / desorption device 51b to the heating fluid W2 or the cooling fluid W3.

  As shown in FIG. 3, when the adsorption process is performed in the first adsorption / desorption device 51a and the desorption process is performed in the second adsorption / desorption device 51b, the first adsorption / desorption device 51a has a cold / hot supply line. L51a is connected, and the cold / hot heat supply line L51b is connected to the 2nd adsorption / desorption device 51b. As shown in FIG. 4, when the desorption process is performed in the first adsorption / desorption device 51a and the adsorption process is performed in the second adsorption / desorption device 51b, the first adsorption / desorption device 51a has cold / hot heat. A supply line L51b is connected, and a cold / hot heat supply line L51a is connected to the second adsorption / desorption device 51b.

  The refrigerant condenser 53 condenses the refrigerant vapor as the refrigerant vapor desorbs from the adsorbent K. The refrigerant condenser 53 exchanges heat between the refrigerant vapor desorbed from the adsorbent K of the first adsorption / desorption device 51a or the second adsorption / desorption device 51b and the cooling fluid W3 flowing through the downstream cooling fluid line L72. The refrigerant vapor is condensed. The condensed refrigerant is recovered in the refrigerant liquid recovery tray 531 as the refrigerant liquid W52. The recovered refrigerant liquid W52 flows down toward the refrigerant liquid spray pipe L521 (described later) via a second spray line L53 (described later), and is stored as the refrigerant liquid W51 at the bottom of the evaporator 52.

  The evaporator 52 evaporates the refrigerant liquid as the refrigerant vapor is adsorbed on the adsorbent K. The evaporator 52 has a refrigerant liquid spray pipe L521 for spraying the refrigerant liquid W51. The refrigerant liquid spraying pipe L521 is arranged on the upper side inside the evaporator 52, and sprays the refrigerant liquid W51 on an evaporator internal line L102 (described later) through which the supply water W10 for producing cold water flows. The refrigerant liquid W51 in contact with the evaporator internal line L102 absorbs latent heat from the supply water W10 and is vaporized. The refrigerant liquid W51 that has not been vaporized is stored again in the bottom of the evaporator 52.

  The upstream end of the refrigerant liquid spray pipe L521 is connected to the bottom of the evaporator 52 via the first spray line L52 at the connection portion J4, and the refrigerant is condensed via the second spray line L53. It is connected to the bottom of the refrigerant liquid recovery tray 531 of the vessel 53. The first spray line L52 is provided with a coolant liquid pump 56 that sends out the coolant liquid W51 accumulated at the bottom of the evaporator 52 toward the coolant liquid spray pipe L521.

  A part of the cold water production line L100 is arranged inside the evaporator 52. The evaporator 52 cools the supply water W10 with the heat of vaporization when the refrigerant liquid is vaporized in the evaporator 52, and manufactures the cold water W11. In the evaporator 52, cold water W11 having a temperature of 10 ° C. or less can be produced from the normal temperature supply water W10.

  The cold water production line L100 is a line for circulating water to the cold water use facility 11 (for example, an air conditioner for cooling). A part of the cold water production line L100 is disposed inside the evaporator 52. The cold water production line L100 includes a supply water line L101 serving as a return path for circulating water, an evaporator internal line L102 for cooling the circulating water, and a cold water line L103 serving as an outbound path for circulating water. Although depending on the cooling capacity of the adsorption refrigeration machine 5 and the amount of heat absorbed by the cold water use facility 11, the temperature of the cold water W11 flowing through the cold water line L103 is about 5 to 10 ° C. and flows through the supply water line L101. The temperature of the supply water W10 is about 15 to 35 ° C.

  The supply water W10 supplied to the evaporator 52 flows through the supply water line L101. The upstream end of the supply water line L101 is connected to the water outlet of the cold water use facility 11. The downstream end of the feed water line L101 is connected to the upstream end of the evaporator internal line L102 in the evaporator 52.

  The evaporator internal line L102 is disposed inside the evaporator 52. The supply water W10 supplied from the supply water line L101 flows into the evaporator internal line L102, and cold water W11 is produced from the supply water W10 by heat of vaporization when the refrigerant is vaporized in the evaporator 52. The cold water W11 produced in the evaporator internal line L102 flows out to the cold water line L103. The upstream end of the evaporator internal line L102 is connected to the downstream end of the feed water line L101. The downstream end of the evaporator internal line L102 is connected to the upstream end of the cold water line L103.

  In the cold water line L103, cold water W11 sent from the evaporator internal line L102 to the cold water use facility 11 flows. The upstream end of the cold water line L103 is connected to the downstream end of the evaporator internal line L102 in the evaporator 52. The downstream end of the cold water line L103 is connected to the water inlet of the cold water use facility 11.

  The evaporator 52 configured as described above evaporates the refrigerant liquid by exchanging heat between the refrigerant liquid W51 sprayed from the refrigerant liquid spray pipe L521 and the supply water W10 flowing through the supply water line L101. Thus, refrigerant vapor that is adsorbed by the adsorbent K of the adsorption / desorption devices 51a and 51b is generated. The evaporator 52 exhibits the refrigerating capacity by utilizing the heat of vaporization of the refrigerant liquid W51, and cools the supply water W10 flowing through the supply water line L101 in the evaporator internal line L102 to produce the cold water W11. The cold water W11 produced by the evaporator 52 in the evaporator internal line L102 is sent to the cold water use facility 11 through the cold water line L103.

As shown in FIGS. 3 and 4, the heating fluid line L6 is connected to the adsorption / desorption devices 51a and 51b in which the desorption process is performed. In the desorption process, the heating fluid W2 for giving warm heat to the adsorbents K of the adsorption / desorption devices 51a and 51b circulates in the heating fluid line L6. As the heating fluid W2, for example, warm water in which water is heated can be used.
In the present embodiment, the heating fluid line L6 is a line through which the heating fluid W2 (hot water) exchanged with the off-gas G1 by the first heat exchanger 3 circulates.

  As shown in FIGS. 2 to 4, the heating fluid line L <b> 6 starts from the first heat exchanger 3, the heat exchange line L <b> 60 disposed inside the first heat exchanger 3, the pre-stage heating fluid line L <b> 61, This is a pipe line in which the cold / hot heat supply line L51 (L51a, L51b) and the subsequent heating fluid line L62 are connected in a loop. Between the upstream heating fluid line L61 and the cool / heat supply line L51 (L51a, L51b), in order to introduce the heating fluid W2 into the adsorption / desorption devices 51a, 51b, the upstream heating fluid line L61 and the cool / heat supply line L51 ( An introduction side switching valve 71 (flow path switching control valve 7) that connects L51a and L51b) is disposed. Between the cool / heat supply line L51 (L51a, L51b) and the rear heating fluid line L62, in order to derive the heating fluid W2 from the adsorption / desorption devices 51a, 51b, the cool / heat supply line L51 (L51a, L51b) and the rear heating fluid line L62. A lead-out side switching valve 72 (flow path switching control valve 7) that connects the heating fluid line L62 is disposed.

  The pre-stage heating fluid line L61 is a line from the first heat exchanger 3 to the flow path switching control valve 7, as shown in FIGS. The upstream end of the upstream heating fluid line L61 is connected to the outlet end of the heat exchange line L60 in the first heat exchanger 3, as shown in FIG. The downstream end of the upstream heating fluid line L61 is connected to the introduction side switching valve 71 of the flow path switching control valve 7, as shown in FIGS. As shown in FIGS. 2 to 4, the upstream heating fluid line L <b> 61 is provided with a connecting portion J <b> 2, a circulation pump 31, and a second heat exchanger 8 in order from the upstream side toward the downstream side. A downstream end portion of a heating fluid bypass line L8 described later is connected to the connection portion J2.

  The circulation pump 31 is a device that circulates the heating fluid W2 flowing through the heating fluid line L6. The circulation pump 31 is supplied with driving power whose frequency is converted from the inverter 32. Circulation pump 31 is driven at a rotational speed corresponding to the frequency (hereinafter also referred to as “drive frequency”) of the supplied (input) drive power. The circulation pump 31 can adjust the rotation speed by an inverter 32.

  The inverter 32 is an electric circuit (or a device having the circuit) that supplies the circulating pump 31 with driving power whose frequency has been converted. A command signal is input from the control unit 10 to the inverter 32. The inverter 32 outputs driving power having a driving frequency corresponding to the frequency designation signal (current value signal or voltage value signal) input by the control unit 10 to the circulation pump 31.

  The second heat exchanger 8 exchanges heat between the heating fluid W2 flowing through the upstream heating fluid line L61 on the upstream side of the adsorption / desorption device 51 and the cooling fluid W32 flowing through the second branch cooling fluid line L92 described later. I do. That is, the second heat exchanger 8 transmits the heat of the heating fluid W2 flowing through the upstream heating fluid line L61 on the upstream side of the adsorption / desorption device 51 to the cooling fluid W32 flowing through the second branch cooling fluid line L92.

  As shown in FIGS. 3 and 4, the cold / hot heat supply line L51 (L51a, L51b) is passed from the introduction side switching valve 71 of the flow path switching control valve 7 via the adsorption / desorption device 51 (51a, 51b). This is a line up to the derivation side switching valve 72. The cold / hot heat supply line L51 (L51a, L51b) is provided with second temperature sensors S2a, S2b. The second temperature sensors S2a and S2b measure the temperature of the heating fluid W2 supplied to the adsorption / desorption device 51 (51a and 51b). The cold / hot heat supply line L51 (L51a, L51b) is configured to constitute a part of the heating fluid line L6 or a part of the cooling fluid line L7 by the flow path switching control valve 7 described later. The flow path is switched.

  The post-stage heating fluid line L62 is a line from the flow path switching control valve 7 to the first heat exchanger 3, as shown in FIGS. The upstream end of the rear heating fluid line L62 is connected to the outlet side switching valve 72 of the flow path switching control valve 7, as shown in FIGS. As shown in FIG. 2, the downstream end of the rear heating fluid line L62 is connected to the inlet end of the heat exchange line L60 in the first heat exchanger 3. The second heating control fluid line L62 is provided with a second proportional control three-way valve V12.

  From the middle of the rear heating fluid line L62, a heating fluid bypass line L8 branches off at the second proportional control three-way valve V12. The downstream end of the heating fluid bypass line L8 is connected to the connection portion J2 of the upstream heating fluid line L61. The heating fluid bypass line L8 branches from the rear heating fluid line L62 on the upstream side of the first heat exchanger 3 at the second proportional control three-way valve V12, bypasses the first heat exchanger 3, and the preceding heating fluid line L61. In the connecting portion J2, the first heating fluid line L61 is joined again to the downstream side of the first heat exchanger 3.

  The second proportional control three-way valve V12 is provided in a portion branched to the heating fluid bypass line L8 in the rear heating fluid line L62. The second proportional control three-way valve V12 is configured by a motor valve, and is a valve capable of adjusting the flow rate of the heating fluid W21 flowing through the heating fluid bypass line L8 by adjusting the valve opening degree. That is, the second proportional control three-way valve V12 is a valve that can change the ratio of the flow rate of the heating fluid W21 that diverts from the rear heating fluid line L62 to the heating fluid bypass line L8. Note that the ratio of the flow rate of the heating fluid W21 distributed by the second proportional control three-way valve V12 is 0 (zero). The ratio of the flow rate of the heating fluid W21 that is divided into one of the subsequent heating fluid line L62 and the heating fluid bypass line L8 ). The flow rate of the heating fluid W21 in the second proportional control three-way valve V12 is controlled by a flow rate adjustment signal from the control unit 10.

As shown in FIGS. 3 and 4, the cooling fluid line L7 is connected to the adsorption / desorption devices 51a and 51b in which the desorption process is performed. In the cooling fluid line L7, a cooling fluid W3 for supplying cold heat to the adsorbents K of the adsorption / desorption devices 51a and 51b in the adsorption process circulates and circulates. As the cooling fluid W3, for example, cooling water in which water is cooled can be used.
In the present embodiment, the cooling fluid line L7 is a line through which the cooling fluid W3 (cooling water) cooled by the cooling tower 6 circulates.

  The cooling tower 6 is a facility for cooling the cooling fluid W3 circulating through the cooling fluid line L7. The cooling tower 6 cools the cooling fluid W3 returned after flowing through the adsorption / desorption unit 51, the refrigerant condenser 53, the off-gas condenser 4 and the second heat exchanger 8 of the adsorption refrigerator 5. The cooling tower 6 includes a cooling unit (not shown) that cools the cooling fluid W3 and a storage unit (not shown) that stores the cooling fluid W3.

  1-4, the cooling fluid line L7 starts from the cooling tower 6 and has an internal flow path (not shown) including a cooling section and a storage section of the cooling tower 6, a preceding cooling fluid line L71, This is a pipe line in which the heat supply line L51 (L51a, L51b) and the rear cooling fluid line L72 are connected in a loop. In order to introduce the cooling fluid W3 into the adsorption / desorption devices 51a and 51b between the preceding cooling fluid line L71 and the cooling / heating supply line L51 (L51a, L51b), the preceding cooling fluid line L71 and the cooling / heating supply line L51 ( An introduction side switching valve 71 (flow path switching control valve 7) that connects L51a and L51b) is disposed. Between the cold / hot heat supply line L51 (L51a, L51b) and the rear cooling fluid line L72, the cold / hot heat supply line L51 (L51a, L51b) and the rear stage are used to derive the cooling fluid W3 from the adsorption / desorption devices 51a, 51b. A lead-out side switching valve 72 (flow path switching control valve 7) that connects the cooling fluid line L72 is disposed.

  The pre-stage cooling fluid line L71 is a line from the cooling tower 6 to the flow path switching control valve 7, as shown in FIGS. The upstream end of the upstream cooling fluid line L71 is connected to the cooling tower 6 as shown in FIG. The downstream end of the front cooling fluid line L71 is connected to the introduction side switching valve 71 of the flow path switching control valve 7, as shown in FIGS.

  The cooling / heating supply line L51 (L51a, L51b) is also a cooling / heating supply line L51 (L51a, L51b) of the heating fluid line L6, and as described above, the heating fluid line L6 by the flow path switching control valve 7 (described later). The flow path is switched so as to constitute a part of the cooling fluid line L7. The cool / heat supply line L51 (L51a, L51b) is connected to the adsorption / desorption device from the introduction side switching valve 71 of the flow path switching control valve 7 in the same manner as the description of the cool / heat supply line L51 (L51a, L51b) of the heating fluid line L6. This is a line from 51 (51a, 51b) to the derivation side switching valve 72. The cold / hot heat supply line L51 (L51a, L51b) is provided with second temperature sensors S2a, S2b.

  The post-stage cooling fluid line L72 is a line from the outlet side switching valve 72 of the flow path switching control valve 7 to the cooling tower 6 via the refrigerant condenser 53, as shown in FIGS. The rear-stage cooling fluid line L72 causes the cooling fluid W3 that has flowed out from the outlet-side switching valve 72 of the flow path switching control valve 7 to flow toward the cooling tower 6.

  As shown in FIG. 2 to FIG. 4, the refrigerant of the adsorption refrigeration machine 5 is sequentially supplied from the outlet side switching valve 72 of the flow path switching control valve 7 to the downstream cooling fluid line L72 from the upstream side to the downstream side. A condenser 53, a first proportional control three-way valve V11, a connection portion J31, a third proportional control three-way valve V13, and a connection portion J32 are provided. In the first proportional control three-way valve V11, the first branch cooling fluid line L91 branches from between the outlet side switching valve 72 of the flow path switching control valve 7 and the connection portion J31 in the rear-stage cooling fluid line L72. The second branch cooling fluid line L92 branches from the connection portion J31 and the connection portion J32 in the rear cooling fluid line L72 at the third proportional control three-way valve V13.

  As shown in FIG. 2, the first branch cooling fluid line L91 branches from the rear-stage cooling fluid line L72 at the first proportional control three-way valve V11, and passes through the off-gas condenser 4 and is connected to the rear-stage cooling fluid line at the connection portion J31. Join L72 again. A first check valve V21 is provided in the first branch cooling fluid line L91 on the downstream side of the off-gas condenser 4.

  The first proportional control three-way valve V11 is provided in a portion branched to the first branch cooling fluid line L91 in the rear-stage cooling fluid line L72. The first proportional control three-way valve V11 is configured by a motor valve and is a valve capable of adjusting the flow rate of the cooling fluid W31 flowing through the first branch cooling fluid line L91 by adjusting the valve opening degree. That is, the first proportional control three-way valve V11 is a valve capable of changing the ratio of the flow rate of the cooling fluid W31 that branches from the rear-stage cooling fluid line L72 to the first branch cooling fluid line L91. In addition, the ratio of the flow rate of the cooling fluid W31 distributed by the first proportional control three-way valve V11 is the ratio of the flow rate of the cooling fluid W31 that is divided into one of the rear-stage cooling fluid line L72 and the first branch cooling fluid line L91. It may be (zero). The flow rate of the cooling fluid W31 adjusted by the first proportional control three-way valve V11 is controlled by a flow rate adjustment signal from the control unit 10.

  The second branch cooling fluid line L92 branches from the rear-stage cooling fluid line L72 at the third proportional control three-way valve V13, and rejoins the rear-stage cooling fluid line L72 at the connection portion J32 via the second heat exchanger 8. . A second check valve V22 is provided in the second branch cooling fluid line L92 on the downstream side of the second heat exchanger 8.

  The third proportional control three-way valve V13 is provided in a portion branched to the second branch cooling fluid line L92 in the rear-stage cooling fluid line L72. The third proportional control three-way valve V13 is configured by a motor valve, and is a valve capable of adjusting the flow rate of the cooling fluid W32 flowing through the second branch cooling fluid line L92 by adjusting the valve opening degree. That is, the third proportional control three-way valve V13 is a valve that can change the ratio of the flow rate of the cooling fluid W32 that is branched from the rear-stage cooling fluid line L72 to the second branch cooling fluid line L92. In addition, the ratio of the flow rate of the cooling fluid W32 distributed by the third proportional control three-way valve V13 is the ratio of the flow rate of the cooling fluid W32 that is divided into one of the rear-stage cooling fluid line L72 and the second branch cooling fluid line L92. It may be (zero). The flow rate of the cooling fluid W32 adjusted by the third proportional control three-way valve V13 is controlled by a flow rate adjustment signal from the control unit 10.

As shown in FIGS. 3 and 4, the flow path switching control valve 7 includes an introduction side switching valve 71 and a derivation side switching valve 72.
When the first adsorption / desorption device 51a executes the adsorption process, the flow path switching control valve 7 introduces the cooling fluid W3 into the first adsorption / desorption device 51a as shown in FIG. 71, the flow path is switched so that the upstream end of the cold / hot heat supply line L51a is connected to the downstream end of the pre-stage cooling fluid line L71. Further, in order to derive the cooling fluid W3 from the first adsorption / desorption device 51a, the downstream side end of the cold / hot heat supply line L51a is connected to the upstream side end of the rear cooling fluid line L72 in the outlet side switching valve 72. Switch the flow path as follows.

  Further, when the second adsorption / desorption device 51b executes the desorption process, the flow path switching control valve 7 introduces the heating fluid W2 into the second adsorption / desorption device 51b as shown in FIG. In the switching valve 71, the flow path is switched so that the upstream end of the cold / hot heat supply line L51b is connected to the downstream end of the upstream heating fluid line L61. Further, in order to derive the heating fluid W2 from the second adsorption / desorption device 51b, the downstream end of the cold / hot heat supply line L51b is connected to the upstream end of the rear heating fluid line L62 in the outlet switching valve 72. Switch the flow path as follows.

  Further, when the first adsorption / desorption device 51a executes the desorption process, the flow path switching control valve 7 introduces the heating fluid W2 into the first adsorption / desorption device 51a as shown in FIG. In the switching valve 71, the flow path is switched so as to connect the upstream end of the cold / hot heat supply line L51a to the downstream end of the upstream heating fluid line L61. Further, in order to derive the heating fluid W2 from the first adsorption / desorption device 51a, in the outlet side switching valve 72, the downstream end of the cold / hot supply line L51a is connected to the upstream end of the rear heating fluid line L62. Switch the flow path as follows.

  Further, when the second adsorption / desorption device 51b performs the adsorption process, the flow path switching control valve 7 introduces the cooling fluid W3 into the second adsorption / desorption device 51b as shown in FIG. In the switching valve 71, the flow path is switched so that the upstream end of the cold / hot heat supply line L51b is connected to the downstream end of the upstream cooling fluid line L71. Further, in order to derive the heating fluid W2 from the second adsorption / desorption device 51b, the downstream end of the cooling / heating supply line L51b is connected to the upstream end of the rear cooling fluid line L72 in the outlet switching valve 72. Switch the flow path as follows.

  The cold water production system 1 controls the introduction side switching valve 71 and the derivation side switching valve 72 and also controls the opening and closing of the evaporator side opening / closing valve bodies 54a, 54b and the refrigerant condenser side opening / closing valve bodies 55a, 55b. 3, the first operation state in which the adsorption process is performed in the first adsorption / desorption device 51 a and the desorption process is performed in the second adsorption / desorption device 51 b, and the first adsorption / desorption device 51 a as illustrated in FIG. 4. The operation state can be switched to the second operation state in which the desorption process is performed in step S2 and the adsorption process is performed in the second adsorption / desorption device 51b. In this embodiment, a 1st driving | running state and a 2nd driving | running state are switched every 250 to 300 second, for example, and are performed repeatedly.

The control unit 10 is configured by a microprocessor (not shown) including a CPU and a memory. The control unit 10 controls the cold water manufacturing system 1.
Further, the control unit 10 controls the flow path switching control valve 7 (the introduction side switching valve 71 and the derivation side switching valve 72), and the evaporator side opening / closing valve bodies 54a and 54b and the refrigerant condenser side opening / closing valve body 55a. , 55b is controlled to switch the operation state of the adsorption refrigeration machine 5 repeatedly between a first operation state and a second operation state at regular intervals.

[1] Adjustment of off-gas discharge temperature In order to achieve water self-sustainability of the fuel cell unit 2, the amount of condensed water (improved for generating the reformed gas G4 by adjusting the discharge temperature of the off-gas G2 is adjusted). Quality water) W1 must be generated. Therefore, the control unit 10 controls the first proportional control three-way valve V11 so that the temperature of the off gas G2 measured by the first temperature sensor S1 is lower than the first set temperature. As a result, the flow rate of the cooling fluid W31 flowing through the first branch cooling fluid line L91 is adjusted, and the flow rate of the cooling fluid W31 flowing through the off-gas condenser 4 is adjusted. The first set temperature is set to a temperature at which water self-sustainability of the fuel cell unit 2 can be achieved, and is typically set to less than 55 ° C, preferably 40 to 50 ° C.

[2] Adjustment of Regeneration Temperature of Water Vapor Adsorbent In order to perform the desorption process reliably in the adsorption / desorption device 51 of the adsorption refrigerator 5, the temperature of the heating fluid W2 is adjusted to adjust the adsorbent K (water vapor adsorbent). ) Must be adjusted to the regeneration temperature range. Therefore, the control unit 10 adjusts the temperature of any one of the following (a) to (d) so as to maintain the temperature of the heated fluid W2 measured by the second temperature sensors S2a and S2b in the second set temperature range. Execute control. The second set temperature range is set to a regeneration temperature zone of the water vapor adsorbent (a temperature range where the desorption of the refrigerant vapor occurs). Depending on the brand of the water vapor adsorbent, for example, a range of 53 to 80 ° C. (setting example 1), 63 It is set in the range of -90 ° C (setting example 2), or in the range of 85-100 ° C (setting example 3). In addition, when the temperature of the heating fluid W2 exceeds the upper limit value of the second set temperature range, the activity of the water vapor adsorbent may be lost. In addition, when the temperature of the heating fluid W2 is less than the lower limit value of the second set temperature range, most of the water vapor adsorbent remains unregenerated and may not be able to exhibit the adsorption ability for the refrigerant vapor.

(A) Temperature control example 1
The control unit 10 controls the second proportional control three-way valve V12 so as to maintain the temperature of the heated fluid W2 measured by the second temperature sensors S2a and S2b in the second set temperature range. Thereby, a part or all of the heating fluid W2 bypasses the first heat exchanger 3, and the flow rate of the heating fluid W2 flowing through the first heat exchanger 3 is adjusted. As a result, the heating amount when the heating fluid W2 passes through the first heat exchanger 3 is limited, and the temperature of the heating fluid W2 flowing through the cold / hot heat supply line L51 (L51a, L51b) is the regeneration temperature zone of the water vapor adsorbent. Is adapted to. As will be described later, a configuration example suitable for implementing the temperature adjustment control example 1 is shown in FIG.

(B) Temperature adjustment control example 2
The controller 10 controls the rotational speed of the circulation pump 31 via the inverter 32 so as to maintain the temperature of the heated fluid W2 measured by the second temperature sensors S2a and S2b in the second set temperature range. Thereby, the discharge amount of the circulation pump 31 is increased or decreased, and the flow rate of the heating fluid W2 flowing through the first heat exchanger 3 is adjusted. As a result, the heating amount when the heating fluid W2 passes through the first heat exchanger 3 is limited, and the temperature of the heating fluid W2 flowing through the cold / hot heat supply line L51 (L51a, L51b) is the regeneration temperature zone of the water vapor adsorbent. Is adapted to. As will be described later, a configuration example suitable for implementing the temperature adjustment control example 2 is shown in FIG.

(C) Temperature adjustment control example 3
The control unit 10 controls the third proportional control three-way valve V13 so as to maintain the temperature of the heated fluid W2 measured by the second temperature sensors S2a and S2b in the second set temperature range. Thereby, the cooling fluid W32 is supplied to the second heat exchanger 8, and the heating fluid W2 flowing through the heating fluid line L6 is cooled. As a result, partial cooling is performed according to the heating amount when the heating fluid W2 passes through the first heat exchanger 3, and the temperature of the heating fluid W2 flowing through the cold / hot heat supply line L51 (L51a, L51b) is It is adapted to the regeneration temperature zone of the water vapor adsorbent. As will be described later, a configuration example suitable for implementing the temperature adjustment control example 3 is shown in FIG.

(D) Temperature adjustment control example 4
The control unit 10 controls the fourth proportional control three-way valve V14 so as to maintain the temperature of the heated fluid W2 measured by the second temperature sensors S2a and S2b in the second set temperature range. Thereby, a part or all of the heating fluid W2 bypasses the first heat exchanger 3, and the flow rate of the heating fluid W2 flowing through the first heat exchanger 3 is adjusted. The flow rate of the off gas G12 flowing through the off gas bypass line L4 is adjusted, and the flow rate of the off gas G1 flowing through the first heat exchanger 3 is adjusted. As a result, the heating amount when the heating fluid W2 passes through the first heat exchanger 3 is limited, and the temperature of the heating fluid W2 flowing through the cold / hot heat supply line L51 (L51a, L51b) is the regeneration temperature zone of the water vapor adsorbent. Is adapted to. As will be described later, a configuration example suitable for implementing the temperature adjustment control example 4 is shown in FIG.

[Configuration Example for Executing Temperature Adjustment Control Examples 1 to 4]
When executing any one of such temperature adjustment control examples 1 to 4, it is not necessary to provide all the configurations of the configuration of the present embodiment, and the configurations necessary for the temperature adjustment control examples 1 to 4 to be adopted. Is selected and adopted. For example, in the configuration of the present embodiment, according to the temperature adjustment control examples 1 to 4 employed, as shown in FIGS. 5 to 8 corresponding to FIG. 2 of the embodiment, the following (i) to (iv) Either configuration example is adopted. However, what is necessary is just to have the structure according to the temperature adjustment control examples 1-4 to employ | adopt, and in addition to the structure example of following (i)-(iv), it does not inhibit further providing another structure. .
FIG. 5 is a flowchart for explaining a first configuration example changed from the configuration shown in FIG. FIG. 6 is a flowchart for explaining a second configuration example changed from the configuration shown in FIG. 2. FIG. 7 is a flowchart for explaining a third configuration example changed from the configuration shown in FIG. FIG. 8 is a flowchart for explaining a fourth configuration example changed from the configuration shown in FIG.

(I) First Configuration Example The first configuration example is a configuration example in the case where the temperature adjustment control example 1 is executed. When the temperature control example 1 is executed, the second proportional control three-way valve V12 and a configuration associated therewith are required, while a configuration other than the second proportional control three-way valve V12 and the configuration associated therewith is provided. It does not have to be.
Specifically, as shown in FIG. 5, the first configuration example includes a second proportional control three-way valve V12 and a heating fluid bypass line L8 in the configuration of the embodiment shown in FIG.
On the other hand, in the first configuration example, in the configuration of the embodiment, the upstream heating fluid line L61 is not provided with the circulation pump 31, and the inverter 32 that controls the circulation pump 31 is not provided. The first configuration example does not include the third proportional control three-way valve V13, the second branch cooling fluid line L92, the second heat exchanger 8, and the second check valve V22 in the configuration of the embodiment. The first configuration example does not include the fourth proportional control three-way valve V14 and the off-gas bypass line L4 in the configuration of the embodiment.

(Ii) Second Configuration Example The second configuration example is a configuration example in the case where the temperature adjustment control example 2 is executed. When the temperature adjustment control example 2 is executed, the configuration of the circulation pump 31 and the inverter 32 is required, but the configuration other than the configuration of the circulation pump 31 and the inverter 32 may not be provided.
Specifically, as shown in FIG. 6, the second configuration example includes a circulation pump 31 and an inverter 32 in the configuration of the embodiment.
On the other hand, in the second configuration example, the second proportional control three-way valve V12 and the heating fluid bypass line L8 are not provided in the configuration of the embodiment. The second configuration example does not include the third proportional control three-way valve V13, the second branch cooling fluid line L92, the second heat exchanger 8, and the second check valve V22 in the configuration of the embodiment. The second configuration example does not include the fourth proportional control three-way valve V14 and the off-gas bypass line L4 in the configuration of the embodiment.

(Iii) Third Configuration Example The third configuration example is a configuration example in the case where the temperature adjustment control example 3 is executed. When the temperature adjustment control example 3 is executed, the third proportional control three-way valve V13 and the configuration associated therewith are required, while the configuration other than the third proportional control three-way valve V13 and the configuration associated therewith is provided. It does not have to be.
Specifically, as shown in FIG. 7, the third configuration example includes a third proportional control three-way valve V13, a second branch cooling fluid line L92, a second heat exchanger 8, and the configuration of the embodiment described above. A second check valve V22 is provided.
On the other hand, in the third configuration example, the second proportional control three-way valve V12 and the heating fluid bypass line L8 are not provided in the configuration of the embodiment. In the third configuration example, in the configuration of the embodiment, the upstream heating fluid line L61 is not provided with the circulation pump 31, and the inverter 32 that controls the circulation pump 31 is also not provided. In the third configuration example, the fourth proportional control three-way valve V14 and the off-gas bypass line L4 are not provided in the configuration of the embodiment.

(Iv) Fourth Configuration Example The fourth configuration example is a configuration example in the case where the temperature adjustment control example 4 is executed. When the temperature control example 4 is executed, the fourth proportional control three-way valve V14 and the configuration accompanying it are required, while the configuration other than the fourth proportional control three-way valve V14 and the configuration associated therewith is provided. It does not have to be.
Specifically, as shown in FIG. 8, the fourth configuration example includes a fourth proportional control three-way valve V14 and an off-gas bypass line L4 in the configuration of the embodiment.
On the other hand, the fourth configuration example does not include the second proportional control three-way valve V12 and the heating fluid bypass line L8 in the configuration of the embodiment. In the fourth configuration example, in the configuration of the embodiment, the upstream heating fluid line L61 is not provided with the circulation pump 31, and the inverter 32 that controls the circulation pump 31 is also not provided. The fourth configuration example does not include the third proportional control three-way valve V13, the second branch cooling fluid line L92, the second heat exchanger 8, and the second check valve V22 in the configuration of the embodiment.

Next, operation | movement of the cold water manufacturing system 1 which concerns on this embodiment is demonstrated.
In the cold water production system 1, when power generation is performed in the fuel cell unit 2, the off-gas G1 discharged from the fuel cell unit 2 passes through the first heat exchanger 3 and the off-gas condenser 4, and water self-sustainment is achieved. The off-gas G2 cooled to an achievable temperature is discharged out of the system.

The off-gas condenser 4 circulates the off-gas G1 after flowing through the off-gas line L1 and having been heat-exchanged by the first heat exchanger 3 by the cooling fluid W31 flowing through the first branch cooling fluid line L91, thereby condensing water W1. Is generated. The condensed water W1 generated by being cooled by the cooling fluid W31 is supplied to the reformer 21 as reformed water. In the reformer 21, the steam of the reformed water W1 supplied through the reformed water supply line L22 (described later) and the raw fuel gas G3 supplied through the fuel supply line L31 are reacted on the catalyst. The reformed gas G4 is generated. The generated reformed gas G4 is supplied to the battery stack 20 through the reformed gas supply line L33.
This realizes so-called water self-sustainedness in which the off-gas G1 is cooled to generate the condensed water W1 and reused when the reformed gas W4 containing hydrogen is generated without requiring supply of water from the outside. be able to.

  Further, the adsorption refrigeration machine 5 executes the first operation state shown in FIG. 3 and the second operation state shown in FIG. 4 alternately to execute the cold water W11 from the supply water W10 flowing through the supply water line L101. To manufacture. In this embodiment, a 1st driving | running state and a 2nd driving | running state are switched every 250 to 300 second, for example, and are performed repeatedly.

In the first operation state of the adsorption refrigerator 5 shown in FIG. 3, the adsorption process is executed in the first adsorption / desorption device 51a, and the desorption process is executed in the second adsorption / desorption device 51b.
In the desorption process of the second adsorption / desorption device 51b, the refrigerant vapor is desorbed (released) from the adsorbent K by the heat of the heating fluid W2 flowing through the cold / hot supply line L51b. The heating fluid W2 flowing through the cold / hot heat supply line L51b is generated in the first heat exchanger 3 by using the waste heat of the offgas G1 discharged from the fuel cell unit 2.

  The refrigerant vapor desorbed from the adsorbent K due to the heating of the second adsorption / desorption device 51b reaches the refrigerant condenser 53, and condenses by giving latent heat to the cooling fluid W3 in the process of contacting the latter cooling fluid line L72. The refrigerant liquid W52 generated by the condensation is collected in the refrigerant liquid collection tray 531. The refrigerant liquid W52 collected in the refrigerant liquid collection tray 531 is supplied to the evaporator 52 via the second spray line L53 and the refrigerant liquid spray pipe L521.

  Further, in the adsorption process of the second adsorption / desorption device 51b, the refrigerant vapor is adsorbed (accumulated) on the adsorbent K by the cold heat of the cooling fluid W3 flowing through the cold / hot supply line L51a. The cooling fluid W3 flowing through the cold / hot heat supply line L51a is generated in the cooling tower 6 by evaporating a part of the cooling fluid W3 in contact with the cooling air.

  When the refrigerant liquid pump 56 is driven, the refrigerant liquid W51 stored at the bottom of the evaporator 52 is sprayed to the evaporator internal line L102 via the second spray line L53 and the coolant liquid spray pipe L521. The dispersed refrigerant liquid W51 absorbs latent heat from the supply water W10 and vaporizes in the process of contacting the evaporator internal line L102. The refrigerant vapor generated by the vaporization is adsorbed on the adsorbent K by the cooling of the first adsorption / desorption device 51a. The supply water W10 flowing in from the supply water line L101 is cooled in the process of passing through the evaporator internal line L102, becomes cold water W11, and flows out to the cold water line L103. Thereby, in the evaporator 52, the cold water W11 is continuously manufactured.

  On the other hand, in the second operation state of the adsorption refrigeration machine 5 shown in FIG. 4, the supply of the heating fluid W2 and the cooling fluid W3 to the first adsorption / desorption device 51a and the second adsorption / desorption device 51b is switched, and the second adsorption / desorption device 51a is switched. An adsorption process is performed in the desorber 51b, and a desorption process is performed in the first adsorption / desorption device 51a. The operation of the adsorption refrigerator 5 shown in FIG. 4 in the second operation state is the same as that of FIG. 3 except that the supply of the heating fluid W2 and the cooling fluid W3 to the first adsorption / desorption device 51a and the second adsorption / desorption device 51b is switched. The operation in the second operation state of the adsorption refrigeration machine 5 shown in FIG. For this reason, the description of the operation in the second operation state will be omitted by using the description of the operation in the first operation state.

  During the operation of the cold water production system 1, the control unit 10 includes the first temperature sensor so that the off-gas condenser 4 can generate the amount of condensed water W1 necessary to generate the reformed gas G4. The first proportional control three-way valve V11 is controlled so that the temperature of the off gas G2 measured in S1 is lower than the first set temperature.

  In addition, during the operation of the cold water production system 1, the control unit 10 controls the second temperature sensor S2a so that the temperature of the heating fluid W2 flowing through the cold / hot heat supply line L51 matches the regeneration temperature zone of the adsorbent K. , S2b, one of the temperature control examples 1 to 4 described above is executed so as to maintain the temperature of the heating fluid W2 in the second set temperature range. In the temperature adjustment control, operation is performed so that the desorption process of the adsorption / desorption device 51 is performed reliably, so that the cold water W11 can be continuously manufactured.

According to the cold water manufacturing system 1 which concerns on this embodiment mentioned above, the following effects are acquired, for example.
The cold water production system 1 of the present embodiment includes a fuel cell unit 2, an adsorption / desorption device 51 that can switch between an adsorption process and a desorption process, an evaporator 52, and a refrigerant condenser 53. The adsorption / desorption device 51 includes: A cooling fluid line L7 through which the cooling fluid W3 circulates in the adsorption process and a heating fluid line L6 through which the heating fluid W2 circulates in the desorption process are connected and supplied by heat of vaporization when the refrigerant is vaporized in the evaporator 52. An adsorption refrigeration machine 5 that produces cold water W11 from water W10, a first heat exchanger 3 that performs heat exchange between a heating fluid W2 that flows through a heating fluid line L6 and an offgas G1 that flows through an offgas line L1, An off-gas condenser 4 that cools the off-gas G1 to generate condensed water W1, a cooling tower 6 that cools the cooling fluid W3 that circulates and flows through the cooling fluid line L7, and a cooling fluid la The flow rate of the first branch cooling fluid line L91 branching from the pipe L7 and rejoining the cooling fluid line L7 via the off-gas condenser 4 and the cooling fluid W31 flowing through the first branch cooling fluid line L91. The first proportional control three-way valve V11, the first temperature sensor S1 for measuring the temperature of the offgas G2 flowing through the third offgas line L13 downstream from the offgas condenser 4, and the offgas measured by the first temperature sensor S1. And a control unit 10 that controls the first proportional control three-way valve V11 so that the temperature of G2 is lower than the first set temperature.

  Therefore, the control part 10 adjusts the flow volume of the cooling fluid W31 distribute | circulated to the off-gas condenser 4 so that the temperature of the off-gas G2 discharged | emitted from the off-gas condenser 4 may be less than the 1st preset temperature which can achieve water independence. . As a result, during the power generation of the fuel cell unit 2, the amount of condensed water W1 required for water self-supporting of the fuel cell unit 2 can be reliably generated. Further, during the power generation of the fuel cell unit 2, the waste heat of the offgas G 1 is recovered by the first heat exchanger 3 and used as a driving heat source for the adsorption refrigeration machine 5. Manufacturing can be realized.

  In the present embodiment, the upstream heating fluid line L62 on the upstream side of the first heat exchanger 3 branches off, bypasses the first heat exchanger 3, and the upstream heating on the downstream side of the first heat exchanger 3. The heating fluid bypass line L8 that rejoins the fluid line L61, the second proportional control three-way valve V12 that adjusts the flow rate of the heating fluid W21 that flows through the heating fluid bypass line L8, and the heating fluid W2 that is supplied to the adsorption / desorption device 51 Second temperature sensors S2a and S2b that measure the temperature of the heating fluid W2 measured by the second temperature sensors S2a and S2b so as to maintain the temperature within the second set temperature range. The second proportional control three-way valve V12 is controlled.

  Therefore, the control unit 10 controls the second proportional control three-way valve V12 so that part or all of the heating fluid W2 bypasses the first heat exchanger 3, and the heating fluid W2 flowing through the first heat exchanger 3 is controlled. Adjust the flow rate. Thus, since the temperature of the heating fluid W2 flowing through the cold / hot heat supply line L51 is operated so as to be adapted to the regeneration temperature zone of the adsorbent K, continuous cold water production by the adsorption refrigerator 5 is realized. Can do.

  In the present embodiment, the second temperature sensor that measures the temperature of the circulating fluid 31 that is provided in the heating fluid line L6 and whose rotation speed can be adjusted by the inverter 32, and the heating fluid W2 that is supplied to the adsorption / desorption device 51. S2a and S2b, and the controller 10 controls the circulation pump 31 via the inverter 32 so as to maintain the temperature of the heated fluid W2 measured by the second temperature sensors S2a and S2b in the second set temperature range. Control the rotation speed.

  Therefore, the control unit 10 controls the rotational speed of the circulation pump 31 so as to increase or decrease the discharge amount, and adjusts the flow rate of the heating fluid W2 flowing through the first heat exchanger 3. Thus, since the temperature of the heating fluid W2 flowing through the cold / hot heat supply line L51 is operated so as to be adapted to the regeneration temperature zone of the adsorbent K, continuous cold water production by the adsorption refrigerator 5 is realized. Can do.

  In the present embodiment, the second branch cooling fluid line L92 branched from the cooling fluid line L7 and joined again to the cooling fluid line L7, and the heating through the cold / hot heat supply line L51 upstream of the adsorption / desorption device 51 are heated. The flow rate of the second heat exchanger 8 that exchanges heat between the fluid W2 and the cooling fluid W32 that flows through the second branch cooling fluid line L92 and the flow rate of the cooling fluid W32 that flows through the second branch cooling fluid line L92 are adjusted. A third proportional control three-way valve V13, and a second temperature sensor for measuring the temperature of the heated fluid W2 supplied to the adsorption / desorption device 51, and the control unit 10 measures the second temperature sensors S2a and S2b. The third proportional control three-way valve V13 is controlled so as to maintain the temperature of the heated fluid W2 in the second set temperature range.

  Therefore, the control unit 10 controls the third proportional control three-way valve V13 so that the cooling fluid W32 is supplied to the second heat exchanger 8, and cools the heating fluid W2 flowing through the heating fluid line L6. Thus, since the temperature of the heating fluid W2 flowing through the cold / hot heat supply line L51 is operated so as to be adapted to the regeneration temperature zone of the adsorbent K, continuous cold water production by the adsorption refrigerator 5 is realized. Can do.

  Moreover, in this embodiment, it branches from the 1st off gas line L11 of the upstream of the 1st heat exchanger 3, bypasses the 1st heat exchanger 3, and is the downstream of the 1st heat exchanger 3. An off-gas bypass line L4 that rejoins the second off-gas line L12 upstream of the off-gas condenser 4, a fourth proportional control three-way valve V14 that adjusts the flow rate of the off-gas G12 that flows through the off-gas bypass line L4, and an adsorption / desorption device 51 And a second temperature sensor S2a, S2b for measuring the temperature of the heated fluid W2 supplied to the controller 10. The control unit 10 sets the temperature of the heated fluid W2 measured by the second temperature sensor S2a, S2b to a second setting. The fourth proportional control three-way valve V14 is controlled so as to maintain the temperature range.

  Therefore, the control unit 10 controls the fourth proportional control three-way valve V14 so that part or all of the heating fluid W2 bypasses the first heat exchanger 3, and the heating fluid W2 flowing through the first heat exchanger 3 is controlled. Adjust the flow rate. Thus, since the temperature of the heating fluid W2 flowing through the cold / hot heat supply line L51 is operated so as to be adapted to the regeneration temperature zone of the adsorbent K, continuous cold water production by the adsorption refrigerator 5 is realized. Can do.

The preferred embodiments of the present invention have been described above. However, the present invention is not limited to the above-described embodiments, and can be implemented in various forms.
For example, in the said embodiment, although the cooling unit was comprised with the cooling tower 6, it is not restricted to this, The cooling unit should just be the equipment which can cool water.

  In the embodiment, the first branch cooling fluid line L91 and the second branch cooling fluid line L92 are configured to branch from the cooling fluid line L7 on the upstream side of the cooling tower 6 (cooling unit). However, it may be configured to branch from the cooling fluid line L7 on the downstream side of the cooling tower 6 (cooling unit).

  In the embodiment, the first proportional control three-way valve V11 is used as the first flow rate adjusting unit, the second proportional control three-way valve V12 is used as the second flow rate adjusting unit, and the third proportional control three-way valve is used as the third flow rate adjusting unit. V13 is a fourth proportional control three-way valve V14 as a fourth flow rate adjusting means. However, the present invention is not limited to this, and two proportional control two-way valves may be used instead of each proportional control three-way valve to adjust the flow rate of the fluid to be divided.

DESCRIPTION OF SYMBOLS 1 Cold water manufacturing system 2 Fuel cell unit 3 1st heat exchanger 4 Off-gas condenser 5 Adsorption-type refrigerator 6 Cooling tower (cooling unit)
8 Second heat exchanger 10 Control unit 31 Circulation pump 32 Inverter 51 Adsorption / desorption device 52 Evaporator 53 Refrigerant condenser A1 Air (oxidant gas)
G1 Off gas G2 Off gas G4 Reformed gas (fuel gas)
K adsorbent L1 Off gas line L13 Third off gas line (off gas line)
L4 Off-gas bypass line L6 Heating fluid line L7 Cooling fluid line L8 Heating fluid bypass line L101 Supply water line L91 First branch cooling fluid line L92 Second branch cooling fluid line S1 First temperature sensor (first temperature measuring means)
S2a, S2b Second temperature sensor (second temperature measuring means)
V11 first proportional control three-way valve (first flow rate adjusting means)
V12 Second proportional control three-way valve (second flow rate adjusting means)
V13 Third proportional control three-way valve (third flow rate adjusting means)
V14 Fourth proportional control three-way valve (fourth flow rate adjusting means)
W2 Heating fluid W3 Cooling fluid W10 Supply water W11 Cold water

Claims (5)

A fuel cell unit that introduces fuel gas and oxidant gas into the battery stack and generates power by electrochemical reaction; and
An adsorption / desorption device that can switch between an adsorption process that adsorbs refrigerant vapor to the adsorbent by cold heat and a desorption process that desorbs refrigerant vapor from the adsorbent by hot heat, and vaporizes the refrigerant liquid when adsorbing the refrigerant vapor to the adsorbent And a refrigerant condenser that condenses the refrigerant vapor as the refrigerant vapor is desorbed from the adsorbent, and the adsorbent / desorber circulates a cooling fluid for applying cold heat to the adsorbent in the adsorption process. A cooling fluid line that circulates, and a heating fluid line that circulates and circulates a heating fluid for applying heat to the adsorbent in the desorption process, and a supply water line through which supply water circulates are connected to the evaporator. An adsorption refrigeration machine for producing cold water from supply water by heat of vaporization when the refrigerant liquid is vaporized in the evaporator;
An offgas line through which offgas discharged from the fuel cell unit flows;
A first heat exchanger that exchanges heat between the heating fluid flowing through the heating fluid line and the offgas flowing through the offgas line;
An off-gas condenser that circulates through the off-gas line and cools off-gas after being heat-exchanged by the first heat exchanger to generate condensed water;
A cooling unit for cooling the cooling fluid circulating through the cooling fluid line;
A first branch cooling fluid line branched from the cooling fluid line and rejoining the cooling fluid line via the off-gas condenser;
First flow rate adjusting means for adjusting the flow rate of the cooling fluid flowing through the first branch cooling fluid line;
First temperature measuring means for measuring the temperature of off-gas flowing through the off-gas line downstream of the off-gas condenser;
And a control unit that controls the first flow rate adjusting means so that the temperature of the off-gas measured by the first temperature measuring means is lower than a first set temperature. A heating fluid bypass that branches from the heating fluid line upstream of the first heat exchanger, bypasses the first heat exchanger, and rejoins the heating fluid line downstream of the first heat exchanger. Line,
Second flow rate adjusting means for adjusting the flow rate of the heating fluid flowing through the heating fluid bypass line;
Second temperature measuring means for measuring the temperature of the heated fluid supplied to the adsorption / desorption device,
The control unit controls the second flow rate adjusting unit so as to maintain the temperature of the heated fluid measured by the second temperature measuring unit in a second set temperature range;
The cold water manufacturing system according to claim 1. A circulation pump provided in the heating fluid line and capable of adjusting a rotation speed by an inverter;
Second temperature measuring means for measuring the temperature of the heated fluid supplied to the adsorption / desorption device,
The controller controls the rotational speed of the circulation pump via the inverter so as to maintain the temperature of the heated fluid measured by the second temperature measuring means in a second set temperature range;
The cold water manufacturing system according to claim 1. A second branch cooling fluid line branched from the cooling fluid line and rejoining the cooling fluid line;
A second heat exchanger that exchanges heat between the heating fluid flowing through the heating fluid line upstream of the adsorption / desorption device and the cooling fluid flowing through the second branch cooling fluid line;
Third flow rate adjusting means for adjusting the flow rate of the cooling fluid flowing through the second branch cooling fluid line;
Second temperature measuring means for measuring the temperature of the heated fluid supplied to the adsorption / desorption device,
The control unit controls the third flow rate adjusting unit to maintain the temperature of the heated fluid measured by the second temperature measuring unit in a second set temperature range;
The cold water manufacturing system according to claim 1. Branching off from the off-gas line upstream of the first heat exchanger, bypassing the first heat exchanger, the off-gas downstream of the first heat exchanger and upstream of the off-gas condenser An off-gas bypass line that rejoins the line;
A fourth flow rate adjusting means for adjusting a flow rate of the off gas flowing through the off gas bypass line;
Second temperature measuring means for measuring the temperature of the heated fluid supplied to the adsorption / desorption device,
The control unit controls the fourth flow rate adjusting unit to maintain the temperature of the heated fluid measured by the second temperature measuring unit in a second set temperature range;
The cold water manufacturing system according to claim 1.

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