JP4613355B2 - Reactor using self heat exchange type heat exchanger - Google Patents

Description

  The present invention relates to a reactor using a self-heat exchange type heat exchanger, and more particularly to a technique suitable for application to the field of thermal engineering for saving energy consumption and the field of environmental technology for purifying air and exhaust gas. Is.

  As one method for improving the performance of the partition heat exchanger, many attempts have been made to increase the area of the heat transfer body (partition) as much as possible in a limited space capacity. Making the shape of the heat transfer body into a bellows type is typical as one of the methods. In addition, as another method for improving the performance, the flow directions of two fluids are aligned with the parallel flow toward the same direction or the counterflows in opposite directions with the heat transfer surface interposed therebetween. In order to realize such a flow, heat exchangers such as a multi-tubular cylindrical structure, a plate structure in which a large number of press-formed heat transfer plates are stacked, and a spiral type have been made.

  On the other hand, when heat is exchanged between upstream and downstream for one fluid, the temperature can be changed only in a part of the flow without consuming excessive heat energy, and in various chemical reactions and heat treatment processes. Thermal energy loss can be reduced. Further, as a system in which such a self-heat exchanger and catalyst or burner combustion are integrated, a system using a self-heat exchanger with a spiral structure (reference: 39th Combustion Symposium, presentation number C145, November 2001) 21 to November 23, Yokohama (Non-Patent Document 1)), a method using a rotary heat storage type heat exchanger ("50% reduction in fuel consumption, energy environment design gas burner", Nikkei Sangyo Shimbun, June 2002 March 25 (Non-patent Document 2)), a method using a heat storage chamber heat exchanger that switches the flow path direction at regular intervals (Japanese Patent Laid-Open No. 2001-349524 (Patent Document 1), literature: 39th combustion) Symposium, presentation number C144, November 21 to November 23, 2001 (Yokohama (Non-patent Document 3)) and the like are known.

  However, these various types of heat exchangers still have a problem that the heat exchange area is not sufficient and the manufacture is complicated. There was also room for improvement in terms of heat exchange efficiency and energy consumption.

JP 2001-349524 A The 39th Combustion Symposium, Presentation Number C145, November 21 to November 23, 2001, Yokohama System using rotary heat storage type heat exchanger (“50% reduction in fuel consumption, energy environment design gas burner”, Nikkei Sangyo Shimbun, June 25, 2002 The 39th Combustion Symposium, presentation number C144, November 21 to November 23, 2001, Yokohama

  The present invention has been made in view of the situation of the prior art, and can provide a larger heat transfer area within a limited capacity, is relatively easy to manufacture, and has a dramatic increase in heat exchange efficiency. It is an object of the present invention to provide a reactor using a self-heat exchange type heat exchanger that can bring about an improvement.

According to the present invention, the above problem is solved by the following technical means.
(1) In a reactor using a heat exchanger having a partition type heat transfer body for separating a high temperature fluid and a low temperature fluid,
The heat transfer body of the heat exchanger has a bellows shape, and both fluids are configured to flow counterclockwise along the ridge line direction or the valley line direction mainly in the gap portion of the heat transfer body, the heat transfer body, are those having a filter function that can flow body transmission and diesel particulate, and, in the end portion intersecting the ridges of the bellows portion of the heat transfer member, opposite the the heat transfer body fluid A reactor that is a self-heat-exchange heat exchanger that is not provided with a fluid wrap-around space for wrapping around the gap portion of the bellows portion.
(2) The reactor according to (1), wherein a heating element is provided in the vicinity of the end.
(3) The above (1), wherein a catalyst that promotes an exothermic reaction is supported on a part or all of the surface of the heat transfer body of the heat exchanger, and the reaction component is used as a fluid. Or the reactor as described in (2).
(4) The reactor according to any one of (1) to (3) above, wherein the heat transfer body having a filter function is held and formed in a bellows shape using a spacer structure.

  According to the present invention, a reactor comprising a self-heat exchange type heat exchanger and a heating element that has a large heat exchange surface within a limited capacity, is relatively easy to manufacture, and has dramatically improved heat exchange efficiency. In this case, since the heat transfer body has a filter function, it is possible to provide a reactor in which fine particles floating in the fluid are captured by the heat transfer body and the captured fine particles can be decomposed and removed.

  Hereinafter, the self heat exchange type heat exchanger of the present invention will be described based on preferred reference examples.

(First Reference Example)
FIG. 1 shows a three-dimensional perspective view of a heat exchanger according to a first reference example.
The heat exchanger of this reference example has a bellows type heat transfer body (BF). The bellows type heat transfer body (BF) has a bellows type (bellows type or accordion type) structure with a partition wall separating the high temperature fluid 1 and the low temperature fluid 2 or 2 '. Both end surfaces (A and A ′) intersecting the ridgeline of the bellows portion of the bellows type heat transfer body (BF) are sealed by closely contacting the upper and lower walls of the heat exchanger via a sealing material (not shown). Has been. Further, both end portions (a and a ′) of the heat transfer body (BF) parallel to the ridgeline of the bellows portion are welded or sealed (FIG. 2) with the side walls (C, C ′) constituting both side surfaces of the heat exchanger. It is sealed by being brought into close contact via (not shown). Further, for the front and rear side surfaces (B and B ′) of the heat exchanger facing the ridge line of the heat transfer body (BF), the distance between the ridge line portion of the heat transfer body (BF) and the side surface of the container (B and B ′) is bellows. The two fluid outlets (D, D ′, E, E ′) are located above and below the front and rear side surfaces (B and B ′) opposite to the ridge line of the heat transfer body (BF). It is provided near both ends.

  By adopting the above-described structure, two fluids having different temperatures entering from the front and rear entrances are arranged in parallel with each other in the ridgeline direction of the bellows with the bellows type heat transfer body (BF) being separated. Flow (flow 1 and 2) or counter flow (1 and 2 ') can be realized. Moreover, a large heat transfer area can be obtained in a limited capacity by making the heat transfer body a bellows type structure. In addition, the bellows type heat transfer body is relatively easy to manufacture, and the heat exchange efficiency is dramatically improved.

  Although the triangular wave shape is exemplified here as the cross-sectional shape of the heat transfer body (BF), the shape is not limited to this, and a flat plate shape in which only the wave shape or the ridge portion is semicircular may be used. The heat transfer body (BF) may be formed by bending a foil-like stainless steel, or may be fired after forming a plate-like ceramic material before firing into a bellows shape. In addition, as a method of preventing damage and deformation of the bellows type heat transfer body due to external compressive force, the surface of the foil-like stainless steel or the plate-like ceramic before firing is made uneven, or a corrugated plate is formed on the corrugated line of the wave. It may be bent in a direction perpendicular or non-parallel to a bellows type so that adjacent bellow surfaces are in contact with each other.

  FIG. 2A is a front perspective view of the structure shown in FIG. D and E are the entrances and exits of the fluid 1 as in FIG. On the back side of each, there are provided entrances and exits D ′ and E ′ for the fluid 2. Further, b and b 'are the ridge line and valley line of the bellows type heat transfer body (BF) as viewed from the front. The overall shape of the bellows type heat transfer body (BF) is not limited to the rectangular parallelepiped as shown here. For example, as shown in FIG. 2 (b), the inflow / outflow portion of the fluid is expanded like a fan, It is good also as a form which makes distribution resistance of this part small. Moreover, as shown in FIG.2 (c), the whole bellows type heat-transfer body is good also as a fan type. By doing so, the flow velocity of the fluid can be changed along the flow, and more efficient heat exchange may be achieved.

  Furthermore, it can also be set as a form like FIG. 3 which made the shape of FIG.2 (c) 1 round in the circumferential direction. In this case, the end portions of the heat transfer body (BF) parallel to the ridge line are sealed by means such as welding or contact with each other via a sealing material. Each symbol in FIG. 3 shows each part corresponding to FIG. D, E, D ′, and E ′ are the entrances and exits of the fluids 1 and 2 (2 ′), respectively, as in FIG. 1. By changing the direction of the fluid 2, countercurrent (2 ′) ). In this structure, sealing on the outer and inner cylindrical surfaces A and A 'is necessary. However, by adopting such a cylindrical shape, both end portions (a and a 'in FIG. 1) parallel to the ridgeline of the bellows disappear. For the surfaces B and B ', as in the case of FIG. 1, it is sufficient that the distance between the ridge line portion of the heat transfer (BF) and the side surface of the container is sufficiently smaller than the pitch of the bellows, and sealing is not necessary.

  Moreover, although it is also cylindrical, the structure which has arrange | positioned the bellows type | mold heat exchanger as shown in FIG. 4 is also possible. Each symbol in FIG. 4 also shows each part corresponding to FIG. In this case, the heat transfer body (BF) is placed in a space sandwiched between the outer cylinder B and the inner cylinder B ′. On the end faces (A and A ′) perpendicular to the ridgeline of the heat transfer body (BF), the respective container surfaces and the heat transfer body (BF) are sealed by means such as a sealant. In addition, it is necessary to seal both ends parallel to the ridge line of the heat transfer body (BF) so that the fluid does not leak to the opposite surface of the heat transfer body (BF) by being in close contact with each other or welding. As in the case of the structure of FIG. 3, the seal portion with the container wall at this portion disappears and becomes unnecessary. On the other hand, in the B and B ′ planes, as in the case of FIG. 1, the distance between the ridge line of the heat transfer body (BF) and each plane is sufficient to be sufficiently smaller than the pitch of the bellows on the respective planes. Absent.

(Second reference example)
FIG. 5 shows a heat exchanger according to the second reference example. The heat exchanger of this reference example is a two-fluid partition wall heat exchanger having the structure of FIG. 1, and a pair of fluid inlet / outlet ports (D, D) on opposite sides of the bellows type heat transfer body (BF). Instead of D ′, E, E ′), D is the entrance, D ′ is the exit, and one end (A ′) of the heat transfer body (BF) is not tightly sealed, but the entrance (D) A fluid wrapping space (F) is provided to circulate the fluid that has entered from the side to the opposite side of the heat transfer body (BF). The other configuration is the same as that of the first reference example.

  By adopting such a structure, it becomes a self-heat exchange type heat exchanger in which one fluid flows counter-currently between the upstream and downstream sides of the bellows type heat transfer body (BF). Further, by applying the same modification, any of the heat exchangers shown in FIGS. 2, 3 and 4 can be a corresponding self-heat exchanger.

  In addition to the effects of the first reference example, the heat exchanger of this reference example seals piping and fluid as compared to a self-heat exchanger using a conventional heat exchanger structure represented by a multi-tube cylindrical type. Therefore, even if the number of bellows is increased, the whole structure and the sealing structure are not complicated at all, and a self-heat exchanger with extremely high heat exchange efficiency can be obtained.

FIG. 6A is a front perspective view of the structure of the self-heat exchanger of FIG. In the figure, b represents a ridge line, and b ′ represents a valley line (corresponding to the ridge line of the bellows portion on the opposite side).
In the second reference example, the fluid wrapping space portion (F) at which the temperature becomes an extreme value is not necessarily at one place, as shown in FIG. 6B, the center of the heat transfer body (BF) in the ridge line direction. By providing the fluid inlet / outlet (D, D ′) in the part, the fluid flowing in from the inlet (D) is divided in the vertical direction, and the space part (F, F ′ adjacent to the different end face of the heat transfer body (BF), respectively. ), And then merge and exit from the exit (D ′). By doing in this way, the seal | sticker between the heat exchanger (BF) in a surface (A) and a container wall becomes unnecessary.

  Further, FIG. 6 (c) shows a bellows type heat transfer body (BF) having a rectangular parallelepiped shape along the ridgeline direction, with respect to a self-heat exchanger having an inlet / outlet at the center as shown in FIG. The entire shape is formed into an annular shape, and both ends of the heat transfer body (BF) intersecting with the ridge line share the same fluid wraparound space (F). In this modified example, there is an advantage that the seal at the end face of the bellows portion is not required while the space portion (F) where the temperature is an extreme value is provided in one place.

(Third reference example)
Hereinafter, a reactor based on a self-heat exchanger having the structure shown in FIG. 5 will be described.
The reactor shown in FIG. 7 is based on the self-heat exchanger shown in FIG. 5, and is integrated with the self-heat exchanger in which a heating element (heater) or a heat-absorbing element (G) is incorporated in the fluid wrapping space (F). Reactor. In the reactor having such a structure, heat is transferred between an inflowing fluid having a low temperature (high) and an outflowing fluid heated (cooled) through a space portion (F) having a maximum (minimum) temperature. The temperature at the outlet (D ′) with respect to the inlet (D) does not become so high (low) even when the space (F) becomes considerably high (low) (for example, the temperatures at D, F, and D ′ are respectively 20 ° C., 700 ° C., 90 ° C.). The structure having such a structure can be used as a reactor that can reduce the energy (electric power) for heating when it is necessary to heat the fluid to cause a thermal reaction but it is not desired to change the temperature when the fluid is taken out again. Therefore, application to chemical reaction equipment in general can be expected.

<Theoretical estimation of the performance of the third reference example>
The performance of the self-heat exchange reactor of the third reference example shown in FIG. 7 is roughly estimated. If the bent shape of the bellows-shaped ridgeline (or valley) of the heat transfer body (BF) is semicircular and the heat transfer surfaces are parallel to each other, the heat conduction in this case sandwiches the parallel plates. It can be regarded as heat conduction between different fluids. The total area of the bellows surface is A (m ² ), the heat transfer rate from the high-temperature fluid to the low-temperature fluid across this heat transfer surface is K (W / m ² · K), and the distance between adjacent bellows surfaces is d ( m). When the inter-surface distance is d = 10 ⁻³ (= 1 mm), it is expected that the flow in the reactor at a flow velocity of the order of 1 m / s is a laminar flow. In the laminar flow flowing between parallel plates, the heat transfer rate h (W / m ² · K) between the wall surface and each of the high-temperature and low-temperature fluids is such that the heat flux is constant (the countercurrent self-heat exchange reactor is Under this condition)
h = 140/17 × λ / D
Given in. Here, the coefficient 140/17 is a dimensionless number generally called a Nusselt number, and is a value analytically determined under given conditions. λ is the thermal conductivity of the fluid (W / m · K), D is a dimension called the representative length, and D = 2d for a parallel plate
It is. Also,
K = 1 / 2h
It becomes. Summing up these equations, K = 35/17 × λ / d
It becomes. In FIG. 7, assuming that a heating element is used, the heat generation amount is assumed to be Q (W), and the heat capacity flow rate of the fluid (assuming no temperature dependency) is μC _p (J / K · s). When the heat exchanger is ideally radiator other than waste heat is insulated shall no relationship inlet temperature T _i and the outlet temperature T _o of the fluid,
_{T o -T i = Q / (} μC p)
It becomes. Here, μ represents the mass flow rate (kg / s) of the fluid, and C _p represents the constant pressure specific heat (J / kg · K) of the fluid. Also, between the fluid temperature T _ri flowing into the fluid wraparound portion (F) and the fluid temperature _Tro flowing out from the fluid wraparound portion (F), _Tro −T _ri = Q / (μC _p )
Holds. Here, the heat exchange rate φ, which means how much heat is transferred from the high temperature side fluid to the low temperature side fluid,
_{φ = (T ro -T o)} / (T ro -T i)
Defined as
_{φ = (T ro -T o)} / (T ro -T o + T o -T i) = (T ro -T o) / (T ro -T o + Q / (μC p))
And then
μC _p ( _Tro− T _o ) = KA (T _o −T _i ) = 35/17 × λ / d · A · Q / (μC _p )
Than,
φ = (35/17 × λ / d · A) / (μC _p + (35/17 × λ / d · A)) (1)
It becomes.

Using the formula (1), a rectangular thin plate having a length of 1600 mm and a width of 200 mm (that is, A = 0.32 m ² ) is bent into 40 planes at intervals of 40 mm, and the interval between adjacent planes is 1 mm (= d). For the heat transfer body (BF), 20 ° C. air (density ρ = 1.166 kg / m ³ , constant pressure specific heat C _p = 1005 J / kg · K) as the inflow fluid, and λ ( Table 1 shows the results of obtaining the relationship between the air flow velocity v (L / s) and the heat exchange rate φ, assuming that = 0.0257 W / m · K) is constant. In this case, μ is
μ = ρv × 10 ⁻³ (2)
Calculated as

The volume V of the heat exchanger formed into a bellows shape is only about 0.32L. Therefore, the space velocity when v = 1 L / s is 3600 v / V = 111250 h ⁻¹ . Even at such high space velocities, if the heat transfer body (BF) can be bent completely into a parallel plate as assumed in the calculation, the heat exchange rate of 93.5% will be extremely high. Is expected. Similarly, even at higher space velocities of v = 2 L / s (SV = 22,500 h ⁻¹ ) and 3 L / s (SV = 33750 h ⁻¹ ), high heat exchange rates of 87.8% and 82.8% can be obtained, respectively. .

<Performance verification experiment of the third reference example>
Next, Table 2 shows the results of a trial manufacture (No. 1 reactor) having the same dimensions as those in the above calculation example and examining the performance. A stainless steel foil having a thickness of 0.03 mm was used as the heat transfer material. In addition, a Kanthal wire was provided in the fluid wrapping part (F) as a heating element, and about 50 W was generated by energization. Heat exchange performances of 78, 69, and 68% were obtained at v = 1, 2, 3 L / s, respectively.

(4th reference example)
FIG. 8 shows a reactor according to the fourth reference example. In this reactor, heating in the reactor described with reference to FIG. 7 is performed by a catalytic reaction of reaction components contained in the fluid. This reactor is a self-heat exchanger having the structure shown in FIG. 5, and the catalyst (H) is supported on the entire surface of the heat transfer body (BF) or the surface close to the end surface into which the fluid flows, and is integrated with the self-heat exchanger. It is a catalyzed reactor. In this reactor, the self-heat exchange structure having a bellows type heat transfer surface having a high heat exchange rate and the monolithic catalyst support structure are integrated, and as a result, the temperature of the reaction fluid is changed as in the case of FIG. A sufficient temperature for the catalytic reaction can be obtained inside the reactor without increasing so much (for example, the temperatures at D, F, and D ′ are 20 ° C., 300 ° C., and 50 ° C., respectively), realizing a highly efficient and energy-saving reaction. be able to.

<Performance verification experiment of the fourth reference example>
In order to actually verify the performance of the self-heat exchange type catalytic reactor of the fourth reference example, a stainless steel foil having a thickness of 0.03 mm, a width of 200 mm, and a length of 2720 mm is used as a heat transfer body at a distance of 40 mm perpendicular to the longitudinal direction. Were bent into a total of 68 surfaces, and a rectangular parallelepiped-shaped heat transfer body having a total shape of about 40 × 40 × 200 mm as shown in FIG. 5 was produced. At this time, the distance between adjacent surfaces of the folded heat transfer body was about 0.59 mm. Furthermore, after coating the alumina-supported platinum catalyst in a range of about 40 mm in width from the end surface on the side where the fluid of the heat transfer body wraps around in the direction of the fluid inlet / outlet, it was stored in a rectangular parallelepiped container made of stainless steel having a thickness of 0.6 mm. This container was provided with doorways corresponding to D and D ′ in FIG. 5, and air containing a low concentration volatile organic component (VOC) was circulated. Table 3 shows the removal performance and heat exchange performance results of each VOC for this prototype No. 2 device. These VOCs having a concentration of 0.3% or less contained in air at room temperature can be converted into 90% by self-oxidation, ie, self-oxidation, without applying auxiliary heat from outside except during ignition. It was possible to continue to decompose. Regarding toluene, even at a relatively high space velocity of 1.1 L / s (SV = 12400 h ^-1 ), toluene with a concentration of about 0.1% is completely decomposed into CO ₂ and H ₂ O with a removal rate of about 94%. did.

  In paint factories and the like, air pollution due to volatile organic components (so-called VOC, volatile organic compounds) such as toluene and xylene has become a problem. However, if this reactor is used, for example, air containing 0.1% of toluene does not require additional heating energy, and by using an oxidation catalyst such as a platinum catalyst, only the heat generated by catalytic combustion of toluene can be obtained. By utilizing it, it is possible to oxidatively decompose while maintaining the reaction temperature. That is, this reactor can be expected to be applied to an apparatus for treating low concentration volatile organic pollutants in the air.

(5th reference example)
FIG. 9 shows a reactor according to the fifth reference example. In this reactor, in the self-heat exchanger having the structure of FIG. 5, the heat transfer body (BF) has heat storage properties, and further, the entire surface of the heat transfer body (BF) or a region near the fluid inlet / outlet. On the surface, the catalyst (H) for reacting the reaction components contained in the fluid is supported, and the entire surface of the heat transfer body (BF) or the surface of the region close to the end face side of the heat transfer body (BF) into which the fluid wraps, The adsorbent (I) that adsorbs reaction components at a low temperature and desorbs them at a high temperature is supported.

  According to this reactor, under transient reaction conditions in which the fluid temperature gradually increases, while the temperature is low, the adsorbent (I) is captured by adsorbing the reaction components. As the fluid temperature rises, it is heated from the portion near the inlet / outlet of the heat transfer body (BF), but the heating of the side portion where the fluid wraps around is considerably delayed due to the heat storage property of the heat transfer body (BF). For this reason, when the heating reaches the entire heat transfer body (BF) and the adsorbed reaction components are desorbed, the temperature near the fluid outlet is further increased, and the conditions under which the catalytic reaction occurs are achieved. The reaction components are decomposed with high efficiency and do not come out to the discharge side. The reactor having such a structure is suitable as an automobile exhaust gas converter for treating hydrocarbons discharged at the start of the engine, which is easy to come out at the start of the engine and is difficult to process with a conventional catalytic converter due to a low exhaust gas temperature. It is.

(Sixth reference example)
FIG. 10 shows a reactor according to the sixth reference example. This reactor is a reactor integrated with a self-heat exchanger having a heating element (G) having the structure shown in FIG. 7, and a filter (J) capable of trapping fine particles is connected to a heat transfer element (BF) through which fluid flows. The structure is in close contact with the end face.

  According to this reactor, by arranging the filter (J) in the space (F) where the temperature becomes highest, the fine particles composed of carbon or high-boiling organic components that can be decomposed at a high temperature, etc. It becomes a self-regenerating filter trap that can be processed without increasing the heat so much and without applying much thermal energy. Particulate matter (PM) in diesel engine exhaust gas, especially solid carbon content (soot) in the diesel engine exhaust gas, cannot be oxidized and removed promptly unless the temperature is 600 ° C. or higher. Conventionally, there has been a technology for intermittently raising the exhaust gas temperature so far to oxidize (PM) trapped in the filter and regenerate the filter, but the energy (fuel) required for this is considerable. It was. However, according to this reactor, there is an advantage that a temperature at which PM oxidation occurs promptly can be obtained without applying much energy. In this reactor, if a PM oxidation catalyst containing Mo, V, etc. is supported on the filter (J), the temperature to be reached can be lowered to 500 ° C or 400 ° C, resulting in energy loss. Can be further reduced. This reactor can be applied as a self-regenerating diesel particulate filter.

(Seventh reference example)
FIG. 11 shows a reactor according to the seventh reference example. This reactor has a structure in which, in the self-regenerating filter trap described with reference to FIG. 10, heating is performed by a catalytic reaction instead of providing the heating element (G). That is, this reactor is provided with a filter (J) for capturing and removing fine particles on the end face of the heat transfer body (BF) on the side where the fluid flows.

  According to this reactor, the temperature in the filter (J) can be increased to a necessary level by adding as much catalytic reaction components as necessary to the fluid. As in the case of FIG. 10, this reactor can be used as a self-regenerating filter trap for treating PM in diesel engine exhaust gas. By performing the heating by catalytic oxidation of the fuel, the thermal energy utilization efficiency is higher than that through the heating element, so that it is more practical. This reactor can also be applied as a self-regenerating diesel particulate filter.

Hereinafter, a reactor using the self-heat exchange heat exchanger of the present invention will be described based on preferred embodiments.
(First embodiment)
FIG. 12 shows a reactor according to the first embodiment of the present invention. This reactor uses a porous material (K) having a filter function as the heat transfer body (BF) in the self-heat exchanger having the structure shown in FIG. 5, and at the end where the fluid of the heat transfer body (BF) flows. The space (F) is eliminated, and the space between the heat transfer body (BF) and the surface (A ′) is sealed.

  In the reactor having this structure, the fluid entering from the inlet (D) passes through the heat transfer body wall, exits to the opposite surface, and is discharged from the outlet (D '). Meanwhile, fine particles floating in the fluid are trapped on the surface of the heat transfer body. In this reactor, a catalyst that promotes the catalytic oxidation reaction is supported on the heat transfer body (BF), and the reaction components are added to the fluid before entering the reactor, so that the same as in the case of FIG. 8 or FIG. In addition, the heat transfer body / filter itself is heated by the heat generated by the catalytic reaction. Further, the self-heat exchange type channel structure similar to that shown in FIG. The degree of filter regeneration (ease of fluid permeation) can be ascertained by means such as measuring the pressure difference across the reactor, and the heating degree of the reactor can be adjusted until the required level is reached.

  In addition, according to this reactor, an alternating-sealed fine particle filter that has been widely used in the past (FIG. 13, L is a porous wall having a filter function, and M is a plugging material that alternately closes the flow path entrance / exit of the honeycomb structure). It is also possible to obtain a filter area density of the same level as that of the filter. Further, since it has a self-heat exchange capability, it is possible to perform filter regeneration with little waste of heat energy. This reactor can also be applied as a self-regenerating diesel particulate filter.

Hereinafter, the radiation heater using the self-heat exchange type heat exchanger of the present invention will be described based on preferred reference examples.
(Eighth reference example)
A radiant heater based on the self-heat exchanger having the structure shown in FIG. 5 will be described. FIG. 14 shows a radiant heater according to an eighth reference example. In the self-heat exchanger of FIG. 5, this radiant heater has thermal conductivity and thermal radiation in a part of the wall partitioning the combustion burner (N) and the space (F) from the outside in the space (F) where the fluid flows. It has a structure including a heat radiation plate (P) having a high rate. In the present radiant heater, a gas containing a combustion oxidant such as air that reacts with fuel (O) is used as the fluid.

According to this structure, by transferring heat to the combustion exhaust gas has a low inflow body temperature can be a radiant heater less efficient thermal energy discarding the combustion exhaust gas. This radiation heater can be applied as an energy-saving gas combustion heater with little heat energy loss to combustion exhaust gas.

(Ninth Reference Example)
FIG. 15 shows a radiant heater according to a ninth reference example. This radiant heater is a radiant heater using a catalytic reactor integrated with the self-heat exchanger shown in FIG. 8, and the thermal conductivity and heat are applied to a part of the wall that divides the space (F) into which the fluid flows and the outside. It has a structure provided with a heat radiation plate (P) having a high emissivity. In the present radiant heater, a fluid containing a reaction component that undergoes an exothermic reaction by the action of the catalyst is used. Usually, an oxidation catalyst such as platinum is used as the catalyst, and a mixture of hydrocarbon and air is used as the fluid. .

  According to such a structure, most of the exhaust heat carried by the fluid generated by the catalytic reaction is transmitted to the inflow fluid having a low temperature, so that a high-efficiency radiant heater with less waste heat energy to be discarded in the fluid is obtained. Can do. This radiant heater can also be applied as an energy-saving gas combustion heater with little heat energy loss to combustion exhaust gas.

  The reference examples and the embodiments of the present invention have been described above. Next, some typical examples and embodiments obtained by modifying these reference examples will be described.

(10th reference example)
In the tenth reference example, in the second reference example, at least one kind of structural body having air permeability separate from the heat transfer body (BF) is provided in the gap portion of the bellows portion of the heat transfer body (BF). It is sandwiched. This structure is made to serve as a spacer.
In FIG. 16, stainless steel wire mesh pieces (m, m ′) having substantially the same shape as one bent surface of the bellows type heat transfer body (BF) are used as the structure, and these are used as the bellows type heat transfer body (BF). It is sandwiched between all the gaps. By sandwiching such a structure, the heat transfer surface spacing becomes uniform, the heat radiation in the gap portion of the bellows-shaped heat transfer body (BF) is blocked, and the heat insulation in the flow path direction is increased. Effects such that heat transfer through the structure increases between adjacent heat transfer surfaces, the temperature in the direction perpendicular to the flow path becomes uniform, and the mechanical strength of the bellows type heat transfer body (BF) increases. And heat exchange performance and durability can be improved. In order to improve the air permeability and reduce the pressure loss in the heat exchanger, it is necessary to use the one having as large an opening ratio as possible, that is, one having a large mesh interval (opening ratio) with respect to the diameter of the wire used for the net. desirable. The mesh direction may be square with respect to the ridge line (or valley line) of the heat transfer body (BF) as shown in FIG. 16, or may be oblique as shown in FIG. 17 (a). Also, instead of a wire mesh piece having a wire wire cut surface at the end, as shown in FIG. 17B, if a wire wire bent into a loop shape and processed into a wire mesh shape is used, a heat transfer body ( BF) and the filter material shown below can be prevented from being damaged at the end of the wire.

Next, an example of the verification result of the tenth reference example will be shown. Table 4 shows a bellows type heat transfer body in which a stainless steel foil having the same dimensions as the prototype No. 1 device, that is, a thickness of 0.03 mm, a length of 1600 mm, and a width of 200 mm, is bent into 40 planes every 40 mm perpendicular to the length direction. For (BF), an alumina-supported platinum catalyst is supported on both surfaces with a width of about 100 mm in the vicinity of the fluid wrapping side, and a plain woven stainless steel wire mesh (opening ratio: 73.9%) with a wire diameter of 0.45 mm is also provided in the mesh direction. The performance of a self-heat exchange type catalytic reactor (prototype No. 3) in which 39 structures cut into a rectangle of 40 × 175 mm with a square is sandwiched between bellows-shaped gaps is shown. In this case, the gap interval was about 1 mm. For all VOCs, the reaction continued in an auto-oxidative manner under the reaction conditions shown in Table 4. As is clear from the results in Table 3, the heat exchange rate was improved by 10% or more under the same flow rate conditions despite the heat transfer area being about 2/3. In the case of toluene, the heat exchange rate reaches 92% at a flow rate condition of 0.64 L / s. Along with this, the VOC concentration at which catalytic combustion can be continued in an auto-oxidizing manner is remarkably reduced. With toluene under the same flow rate conditions, the reaction proceeds even at a low concentration of 0.023%. In addition, the VOC removal rate is also greatly improved as a whole compared with the prototype No. 2 device. For example, even at a high space velocity (= 32800 h ⁻¹ ) with a flow rate of 2.92 L / s, 0.06% of toluene was completely decomposed into CO ₂ and H ₂ O by autooxidation with a removal rate of 99%.

(Second embodiment)
In the second embodiment, a material having a filter function in the first embodiment is formed into a bellows type heat transfer body (BF) using a spacer structure.
According to the embodiment in which the structure as a spacer is sandwiched between the heat transfer body gaps, a material having a low structural strength, which has been thought to be difficult to use as a heat transfer body, is also used as a bellows type heat transfer body (BF). It becomes possible to do. FIG. 18 shows a bellows-type heat transfer body (FC) that combines a heat-resistant filter cloth (FC) having a function of capturing combustible fine particles such as particulate matter discharged from a diesel engine with the structure (m, m ′). BF) (self-heat exchanger type filter trap). One side of the filter cloth (FC) is expanded by folding one end of the filter cloth (FC) to increase the thickness (R portion in FIG. 18 (a)) and then folding it in a bellows shape and then compressing it laterally. The side gap is closed by the filter cloth (FC) itself at one end in the longitudinal direction of the bellows. This is housed in a rectangular parallelepiped container having a channel entrance and exit, and the end surface of the filter that is not folded back is closed with a suitable sealing material (s in FIG. 18B), and the folded portion (R) of the filter cloth (FC) is outside. A self-heat exchange type filter trap is obtained by close contact between the portion folded back to the heat exchanger container and the heat exchanger container by using a close seal or a suitable sealing material (not shown). That is, FIG. 18B is a front perspective view of this structure, but a fluid (typically combustion exhaust gas) containing combustible fine particles entering from the front side entrance (D) in the figure is a spacer ( m) is moving downward through the front side void where the fine particles are not trapped and the filter cloth (FC) is transmitted through the highly breathable part, and the spacer (m ′) is arranged. It flows upward through the back side gap and is discharged from the back side outlet (D ′). During this time, self-heat exchange is performed between the forward path side and the return path side.

  Further, FIG. 19A shows not only the thickness of one end of a filter cloth (FC) similar to that of FIG. 18A by folding, but also folding the other end to the opposite side to increase the thickness. FIG. 4 is a front perspective view of a self-heat exchanger type filter trap having a bellows shape using a spacer (m: arranged on the front side, m ′: arranged on the back side). In this way, both ends of the bellows-shaped gap are alternately sealed. As a result, the sealing material (s) shown in FIG. 18B becomes unnecessary, and the structure as a self-heat exchange type filter trap can be simplified. Further, in this alternately sealed bellows type heat transfer body (BF), as shown in FIG. 19 (b), the fluid inlet (D) may be brought upward rather than the front side as before. Is possible. The outlet (D ′) is on the back side as in FIG. By setting the entrance at this position, the fluid can easily flow evenly into the plurality of outward passage voids of the bellows-shaped heat transfer body (BF), so that the heat exchange performance and the particulate capturing function are improved. Of course, in this case, the flow path direction may be opposite.

(11th reference example)
In the eleventh reference example, in the second reference example, a functional material such as a catalyst, an adsorbent, a heat storage material, or a filter material is sandwiched in the gap portion of the bellows portion of the heat transfer body (BF). .
In the fourth reference example, the fifth reference example, and the first embodiment, the catalyst, the adsorbent, and the heat storage material are all directly supported by the heat transfer body (BF) or the heat transfer body (BF). However, in this eleventh reference example, these functional materials are sandwiched between the heat transfer body gaps separately from the heat transfer body (BF).

The first of the eleventh reference example is a structure in which a functional material such as a catalyst, an adsorbent, and a heat storage material is supported on the spacer structure used in the tenth reference example.
The second of the eleventh reference example uses a structure that serves both as a spacer and a functional material. For example, it is possible to use a technique in which a pellet-type catalyst having a substantially constant particle size and appropriate mechanical strength is further packed in the gap.
Further, the third of the eleventh reference example includes a functional material sandwiched in addition to the spacer structure.

  Here, a third example of the eleventh reference example is shown in FIG. This example shows the vicinity of the end where the fluid wraps around the bellows type heat transfer body (BF) with the same spacers (m: forward path side and m ′: return path side) as shown in FIG. It is. In this vicinity, an arrangement is shown in which a belt-like heat-resistant cloth (CL) carrying a functional material such as a catalyst is further sandwiched between the heat transfer body (BF) and the spacer (m ′). By sandwiching the functional material separate from the heat transfer body (BF) in this way, it becomes possible to place the functional material only on the forward path or the return path side as a self-heat exchanger, and to improve various performances. Can do.

Further, a demonstration example of the third example (FIG. 20) of the eleventh reference example is shown. Table 5 shows a self-heat exchanger sandwiching a wire mesh structure (m, m ′) having the same dimensions and the same structure as prototype No. 3 except that the catalyst was not supported on the heat transfer body (BF). The performance of a self-heat exchange type catalytic reactor (prototype No. 4) with a heat-resistant cloth (CL) carrying a platinum catalyst, which is 1600mm long and 40mm wide, sandwiched only on the return path near the fluid wrapping end. It is shown. Compared with the results in Table 4, the heat exchange rate under the same conditions is improved by about 2%. Further, regarding ethylene, a high heat exchange rate substantially equal to the theoretical value shown in Table 1 is obtained even at a high space velocity (22300 h ⁻¹ ) with a flow rate of 1.98 L / s. This is presumably because, in addition to the effect of the spacer structure (m, m ′) described above, the catalytic reaction occurs only on the return path side, so that the heat exchange is facilitated upstream (outward path side).

In addition to the prototype No. 4, the mullite heat-resistant cloth (CL) carrying vanadium pentoxide, which has a filter function and also has a carbon oxidation catalyst, is in close contact with the end face of the fluid transfer part (BF). Thus, a prototype No. 5 was produced in which the gas flow direction was opposite to that in Table 5, that is, the catalyst carrier was on the forward path side, and the performance as a self-heat exchange type filter trap was verified. The fluid used here is room temperature air in which 0.1 to 1 mg / L of carbon black is suspended, which simulates diesel exhaust gas. In order to increase the reaction temperature, 1.5% of H ₂ was further added to the air. The flow rate of this mixed gas was 0.33 L / s. As a result, due to the reaction heat and self-exchange function when H ₂ is oxidized on the platinum catalyst, the average temperature _{Tro at} the turn-up portion of this reactor rises to 567 ° C. and the prototype is not captured. Carbon removal rate φ (=) obtained from 0.109 g (= W _C ) of carbon black passed through and 0.175 g (= W _COx ) of incinerated carbon calculated from CO ₂ and CO generated by oxidation of carbon black W _COx / (W _C + W _COx ) × 100) was 62%. In addition, the heat exchange rate calculated _| required from said _Tro , entrance temperature 29 _degreeC ( _Ti ), and exit temperature 123 degreeC (To) was about 83%.

(12th reference example)
The twelfth reference example is a self-heat exchange type heat exchanger having the same function as that of the second reference example, in which a part of the heat transfer body surface is opened and used as a fluid wraparound part.
The fluid wraparound portion (F) of the self-heat exchange type heat exchanger described in the second reference example uses the end face formed by bending the heat transfer body (BF) in a bellows shape as it is. A first modification of the fourth modification is that a part of the heat transfer body end portion is cut to arbitrarily form a boundary and a space around which the fluid flows. A specific example is shown in FIG. In this case, a part of the heat transfer body (BF) is cut into a trapezoidal shape on one bent surface of the bellows type heat transfer body (BF) to form a fluid wraparound portion (Q). Other surfaces may be cut together, or the location may be shifted, or the cut shape may be changed to a triangle, rectangle, or other shape. In this way, the fluid wrap-around space can be formed without providing a gap between the heat transfer body (BF) and the sealing material (s ′).

  The second of the twelfth reference example is that, in the second reference example, an opening having a closed periphery is provided on each bent surface of the heat transfer body (BF), and this is used as a fluid wraparound part. An example is shown in FIG. In this structure, a circular opening (S) is provided at a location away from the fluid inlet / outlet of each bent surface of the bellows type heat transfer body (BF). At this time, the fundamental difference from FIG. 21A is that the opening does not overlap the end of the heat transfer body (BF) and occupies a closed planar region. As shown in the figure, there may be a plurality of openings (S) or a single opening for each folding surface. By providing such an opening (S), a flow path for self-heat exchange can be formed without providing a space for fluid wrapping around the end face of the heat transfer body.

(13th Reference Example)
The thirteenth reference example is a combination of a non-breathable heat transfer body (BF), a spacer structure, and a filter cloth. That is, in the tenth reference example in which the heat transfer body (BF) and the spacer structure (m, m ′: for example, a wire mesh) are combined, the structure is further extended from the end surface of the fluid wrap portion of the heat transfer body (BF). The filter cloth (FC) is formed in a bellows shape around it.
FIG. 22 shows an example of the thirteenth reference example. As shown in FIG. 22 (a), a rectangular spacer (m ′) is sandwiched on the return path side of the heat transfer body (BF) having no air permeability. In that case, it arrange | positions so that the end of spacer (m ') may protrude from the fluid wraparound end surface of a heat exchanger (BF). Next, a filter cloth (FC) having a bellows shape and having a thickness (R) is formed by folding the end portion so as to cover a part of the heat transfer body (BF) and the protruding portion of the spacer (m ′). . Further, the spacer (m) is sandwiched between the outward gaps so as not to overlap with the R portion and to extend over both the filter cloth (FC) and the heat transfer body (BF).
FIG. 22B is a cross-sectional view showing the positional relationship between these components more clearly, taken on a plane perpendicular to the heat transfer surface. Since the filter cloth (FC) extends further from the end face of the heat transfer body (BF) and the tip of the filter cloth (FC) is sealed at the folded part, the fluid is on the return path side with the spacer (m ′) sandwiched through the filter cloth (FC) As a result, it functions as a self-heat exchanger with a filter trap. In addition, it is good also as a system which reverses the folding direction of a filter cloth | cross (FC) and seals the edge part of a return-path side space | gap part (right of FIG.22 (b)).

(14th reference example)
The fourteenth reference example is a self-heat exchange type filter trap in which a heat transfer body (BF) having the shape of the twelfth reference example, a spacer structure (m, m ′), and a filter cloth are combined. FIG. 23 shows two examples of the sixth modification.
In FIG. 23 (a), instead of projecting the spacer from the end of the heat transfer body, a cut portion as shown in FIG. 21 (a) is made at the end of the heat transfer body, and the filter cloth (FC) and the spacer structure ( By arranging m, m ′), a ventilation portion (Q) having a filter function is formed without causing the forward path side spacer (m) to protrude from the end portion of the heat transfer body. If it does in this way, the end surface of a heat exchanger (BF) and a spacer (m) can be arranged, and the assembly as a filter trap becomes easy.
Further, using a heat transfer body (BF) having an opening that does not overlap with the end of the heat transfer body as shown in FIG. 21B, a filter cloth (FC) and a spacer structure as shown in FIG. (M, m ′) may be arranged. In this way, the end faces of the heat transfer body (BF), the filter cloth (FC), and the spacer (m ′) overlap (the end face of the spacer (m) is recessed by R from these), and assembling as a filter trap Is even easier.

It is a three-dimensional perspective view showing the heat exchanger of the first reference example. (A) is a front perspective view of FIG. 1, (b) and (c) are front perspective views of a modification. It is a figure which shows another example of a 1st reference example. It is a figure which shows another example of a 1st reference example. It is a perspective view which shows the heat exchanger which concerns on a 2nd reference example. (A) is front perspective drawing of FIG. 5, (b) and (c) are front perspective views of another example. It is a front perspective view which shows the reactor of the 3rd reference example based on a self-heat exchanger. It is a front perspective view which shows the reactor of the 4th reference example based on a self-heat exchanger. It is a front perspective view which shows the reactor of the 5th reference example based on a self-heat exchanger. It is a front perspective view which shows the reactor of the 6th reference example based on a self-heat exchanger. It is a front perspective view which shows the reactor of the 7th reference example based on a self-heat exchanger. 1 is a front perspective view showing a reactor of a first embodiment based on a self-heat exchanger according to the present invention. FIG. It is explanatory drawing of an alternately sealed type particulate filter. It is a front perspective view of the radiation heater of the 8th reference example based on a self heat exchanger. It is a front perspective view of the radiation heater of the 9th reference example based on a self heat exchanger. It is explanatory drawing of a 10th reference example. It is explanatory drawing of a 10th reference example. It is explanatory drawing of 2nd Example. It is explanatory drawing of 2nd Example. It is explanatory drawing of the 11th reference example. It is explanatory drawing of a 12th reference example. It is explanatory drawing of the 13th reference example. It is explanatory drawing of the 14th reference example.

Explanation of symbols

BF bellows type heat transfer body 1 high temperature fluid 2, 2 ′ low temperature fluid A, A ′ both end surfaces a, a ′ both end portions B, B ′ front and rear side surfaces C, C ′ side walls D, D ′, E, E ′ entrance / exit F fluid Circumferential space G Heat generating element or endothermic element H Catalyst I Adsorbent J Filter K Porous material L Porous wall M Sealing material N Combustion burner O Fuel P Heat radiation plate m, m 'Spacer R Folding part FC Filter cloth CL Cross s, s' sealant S, Q opening

Claims (4)

In a reactor using a heat exchanger having a partition type heat transfer body for separating a high temperature fluid and a low temperature fluid,
The heat transfer body of the heat exchanger has a bellows shape, and both fluids are configured to flow counterclockwise along the ridge line direction or the valley line direction mainly in the gap portion of the heat transfer body, the heat transfer body, are those having a filter function that can flow body transmission and diesel particulate, and, in the end portion intersecting the ridges of the bellows portion of the heat transfer member, opposite the the heat transfer body fluid A reactor that is a self-heat-exchange heat exchanger that is not provided with a fluid wrap-around space for wrapping around the gap portion of the bellows portion.   The reactor according to claim 1, wherein a heating element is provided near the end.   3. The catalyst according to claim 1, wherein a catalyst that promotes an exothermic reaction is supported on a part or all of the surface of the heat exchanger of the heat exchanger, and the reaction component is used as a fluid. Reactor.   The reactor according to any one of claims 1 to 3, wherein the heat transfer body having a filter function is held and formed in a bellows shape using a spacer structure.