CN101373115A - Gas-liquid separator, high temperature regenerator, absorption type refrigerator and absorption type heatpump - Google Patents
Gas-liquid separator, high temperature regenerator, absorption type refrigerator and absorption type heatpump Download PDFInfo
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- CN101373115A CN101373115A CNA2008102140010A CN200810214001A CN101373115A CN 101373115 A CN101373115 A CN 101373115A CN A2008102140010 A CNA2008102140010 A CN A2008102140010A CN 200810214001 A CN200810214001 A CN 200810214001A CN 101373115 A CN101373115 A CN 101373115A
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- 238000010521 absorption reaction Methods 0.000 title claims abstract description 97
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- 239000006096 absorbing agent Substances 0.000 claims description 58
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- 230000008020 evaporation Effects 0.000 claims description 25
- 238000010438 heat treatment Methods 0.000 claims description 19
- 238000005057 refrigeration Methods 0.000 claims description 18
- 239000003795 chemical substances by application Substances 0.000 claims description 16
- 238000002309 gasification Methods 0.000 claims description 8
- 238000001514 detection method Methods 0.000 claims description 4
- 238000009795 derivation Methods 0.000 claims description 3
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- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 description 6
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- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A30/00—Adapting or protecting infrastructure or their operation
- Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/62—Absorption based systems
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- Sorption Type Refrigeration Machines (AREA)
Abstract
The invention provides a small gas-liquid separator with excellent property on gas-liquid separation, a high temperature regenerator provided with the gas-liquid separator, and an absorption refrigerating machine and an absorption heat pump. The gas-liquid separator (20) separates gas (Va) and liquid (Sa) from mixed fluid (Fm) with gas and liquid mixed, comprising a baffle (21) colliding the lead mixed fluid (Fm) so as to separate the liquid (Sa); a baffle (22) separating the internal of the gas-liquid separator (20) into an inlet chamber (28) and an outlet chamber (29), comprising a plate part (24) for colliding the mixed fluid (Fm) from which the liquid (Sa) is separated by use of the baffle (21) so as to separate the liquid (Sa) further; a lead-in opening (28d) is formed in the inlet chamber (28) so as to lead the mixed fluid (Fm); a gas lead-out opening (29e) is formed at the outlet chamber (29) so as to lead the gas (Va) separated from the mixed fluid (Fm) out.
Description
Technical field
The present invention relates to gas-liquid separator, high-temp regenerator and Absorption Refrigerator and absorption heat pump, particularly relate to the gas-liquid separator of small-sized and gas-liquid separation superior performance, the high-temp regenerator that possesses this gas-liquid separator and Absorption Refrigerator and absorption heat pump.
Background technology
In the high-temp regenerator of Absorption Refrigerator, make the refrigerant vapour evaporation by heat dilute solution, and with weak solution regeneration concentrated solution.At this moment, exist for refrigerant vapour being separated with concentrated solution and taking out respectively and have a high-temp regenerator (for example, with reference to patent documentation 1) of gas-liquid separator.As the gas-liquid separator that high-temp regenerator had in the past, following such structure is arranged: be provided with the baffle plate that extends to the centre of gas-liquid separator from the top board of gas-liquid separator cylindraceous to vertical below, upper portion side wall the side in the space on the top of cutting apart by baffle plate, be formed with introducing port, being used for the refrigerant vapour that will separate because of the heating of weak solution and the fluid-mixing of concentrated solution imports, top board the opposing party is formed with export mouth, is used to derive separated refrigerant vapour.In this gas-liquid separator, the fluid-mixing that imports from introducing port, and is risen in the following side space upset of baffle plate towards the below by baffle directs.And, at fluid-mixing since baffle plate and towards below when flowing and when the following side space upset of baffle plate is risen, concentrated solution is separated from fluid-mixing, the refrigerant vapour upset is risen and concentrated solution descends.In addition, the situation (for example, with reference to patent documentation 2) that gas-liquid separator is set is also arranged on the absorption heat pump that takes out steam.
Patent documentation 1: TOHKEMY 2007-085619 communique (Fig. 1 etc.)
Patent documentation 1: TOHKEMY 2006-138614 communique (Fig. 2～5 etc.)
In structure as described above, if reduce to bring into play the size of the gas-liquid separator of effect as described above, then concentrated solution can be sneaked into from the refrigerant vapour that export mouth is derived sometimes, thereby the gas-liquid separation performance descends.Therefore, in the gas-liquid separator of structure as described above, in order from fluid-mixing, to separate refrigerant vapour fully, and take out refrigerant vapour and concentrated solution, and have to strengthen the size shape of gas-liquid separator, thereby be difficult to adapt to the requirement of miniaturization.
The present invention is in view of above-mentioned problem, purpose is to provide, the gas-liquid separator of small-sized and gas-liquid separation superior performance, small-sized and can take out the high-temp regenerator of the refrigerant vapour of abundant separation and concentrated solution, small-sized and Absorption Refrigerator and absorption heat pump that efficient is high.
Summary of the invention
To achieve these goals, the gas-liquid separator that first mode of the present invention relates to, for example shown in Figure 1, divided gas flow Va and liquid Sa the fluid-mixing Fm that has obtained from having mixed gas Va and liquid Sa, this gas-liquid separator 20 possesses: baffle plate 21 is used to make the fluid-mixing Fm and its collision and the separating liquid Sa that are imported; Dividing plate 22, it will be divided into inlet 28 and downstream chamber 29 in the gas-liquid separator 20, wherein inlet 28 is formed with the introducing port 28d that is used to import fluid-mixing Fm, downstream chamber 29 is formed with the gas export mouth 29e that is used for deriving from fluid-mixing Fm gas separated Va, this dividing plate 22 comprises plate-shaped member 24 and constitutes, and this plate-shaped member 24 is used to make fluid-mixing Fm and its collision that utilizes baffle plate 21 and separated liquid Sa, comes further separating liquid Sa.
According to such formation, comprise the dividing plate that plate-shaped member constitutes owing to possessing, therefore the liquid that has not been separated by baffle plate can be separated by plate-shaped member, also can gas be separated fully with liquid even reduce the size of gas-liquid separator, thereby become gas-liquid separator small-sized and the gas-liquid separation superior performance at the plate-shaped member place.
In addition, the gas-liquid separator that second mode of the present invention relates to, for example shown in Figure 1, on the basis of the gas-liquid separator 20 that first mode of the invention described above relates to, baffle plate 21 constitutes with dividing plate 22 one; Bottom in inlet 28 and downstream chamber 29 is formed with the connected entrance 27 that is communicated with inlet 28 and downstream chamber 29; Below the lower end of introducing port 28d and be formed at downstream chamber's 29 sides of the peristome 23 of dividing plate 22, arrange along the face of dividing plate 22 and be equipped with a plurality of plate-shaped members 24.At this, peristome 23, typically, the more mode of the position of below that is positioned at the lower end of introducing port 28d with its upper end is formed at dividing plate 22.
According to such formation, because below the lower end of introducing port and be formed at downstream chamber's side of the peristome of dividing plate, face arrangement along dividing plate is equipped with a plurality of plate-shaped members, therefore thereby the mixed flow that is imported into is known from experience along baffle plate decline liquid separated, liquid is further separated during the gap of the plate-shaped member that sets by a plurality of arrangements at fluid-mixing, thereby gas can be separated fully with liquid, become gas-liquid separator small-sized and the gas-liquid separation superior performance.
In addition, the gas-liquid separator that Third Way of the present invention relates to, for example shown in Figure 1, on the basis of the gas-liquid separator 20 that second mode of the invention described above relates to, plate-shaped member 24 is to set in the roughly vertical mode of crest line that forms by bending.
According to such formation,, therefore can improve gas-liquid separation effect because the liquid that is separated by plate-shaped member drops onto the below along the plane of plate-shaped member.
In addition, the gas-liquid separator that cubic formula of the present invention relates to, for example shown in Figure 1, in first mode of the invention described above to the basis of the related gas-liquid separator 20 of any one mode in the Third Way, possesses liquid level detector 26, this liquid level detector 26 detects the liquid level that is stored in the liquid Sa in the gas-liquid separator 20 and sends signal to the control device 65 (for example referring to Fig. 3) of the liquid level that is used to control the liquid Sa gas-liquid separator 20 in, to keep connected entrance 27 to submerge being stored in the state among the interior liquid Sa of gas-liquid separator 20.Wherein, so-called connected entrance 27 submerges among the liquid Sa, and the upper end that is meant connected entrance 27 is positioned at the state of below of the liquid level of liquid Sa.
According to such formation,, therefore can make the stability of flow of the liquid that from gas-liquid separator, takes out owing to possess the liquid level detector of the liquid level that is used for detecting the liquid that is stored in gas-liquid separator.In addition, because the liquid level of the liquid of control in the gas-liquid separator is to keep connected entrance to submerge being stored in the state in the liquid in the gas-liquid separator, even therefore the importing owing to fluid-mixing makes the liquid that is stored in inlet's side produce wave, also can suppress to be stored in the wave of liquid of the bottom of downstream chamber's side by the dividing plate that comprises plate-shaped member, thereby can make the detection of liquid level stable.
To achieve these goals, the high-temp regenerator that the 5th mode of the present invention relates to, for example shown in Figure 2, gas Va is the refrigerant vapour that produces by heat dilute solution Sw; Liquid Sa is to produce the concentrated solution that refrigerant vapour Va makes concentration rise and obtain by heat dilute solution Sw; In addition, possess the related gas-liquid separator 20 of any one mode in the cubic formula of first mode to the of the invention described above and hold the liquid chamber 14 of weak solution Sw, in the bottom of gas-liquid separator 20, be formed with phegma export mouth 20r, be used for separated concentrated solution Sr is derived to liquid chamber 14.
Usually, high-temp regenerator takes out the concentrated solution of ormal weight with the refrigerant vapour that is produced, and is included in the liquid in the fluid-mixing before separating, more than being the situation of the boiler of purpose with gas-liquid separator etc. to take out gas.The formation of the high-temp regenerator that the 5th mode according to the present invention relates to, become the high-temp regenerator that possesses following gas-liquid separator, this gas-liquid separator is, for example, usually, because at the cold-producing medium that is adopted is water, solution is under the situation of lithium bromide water solution, the bigger characteristic of proportion with solution, so dripping owing to the effect of gravity and promote, the concentrated solution that is comprised in the fluid-mixing separates, therefore, can take out the refrigerant vapour that has separated concentrated solution fully, and also be suitable for taking out concentrated solution.In addition, owing to possess the related gas-liquid separator of any one mode in the cubic formula of first mode to the of the invention described above, therefore can make high-temp regenerator small-sized and take out refrigerant vapour and concentrated solution after separating fully.In addition, because in the bottom of gas-liquid separator, be formed with and be used for phegma export mouth that separated concentrated solution is derived to liquid chamber, therefore when having little time the concentrated solution from high-temp regenerator derived, can make remaining concentrated solution be back to liquid chamber.
To achieve these goals, the Absorption Refrigerator that the 6th mode of the present invention relates to, for example shown in Figure 3, possess: the high-temp regenerator 32A that the 5th mode of the invention described above relates to; Condenser 33, refrigerant vapour Vb is used to condense; Evaporimeter 34, it imports the refrigerant liquid Vf that condenses in condenser 33, and utilizes the heat of the medium p that is cooled to make refrigerant liquid Vf evaporation; Absorber 31, it imports concentrated solution Sc, and will concentration be reduced with the cold-producing medium Ve that concentrated solution Sc is absorbed in evaporation in the evaporimeter 34 and the weak solution Sw that obtains derives to liquid chamber 14 (for example referring to Fig. 2).For " weak solution is derived to liquid chamber 14 ", just weak solution is not directly guided to the situation of liquid chamber from absorber at this, but also comprise the situation that guides to liquid chamber by the regenerator beyond the above-mentioned high-temp regenerator.In addition, for the concentrated solution that absorber imports, just will directly not import the situation of absorber, but also comprise the situation that imports to absorber by the regenerator beyond the above-mentioned high-temp regenerator from the concentrated solution that above-mentioned high-temp regenerator is derived.
According to such formation, owing to possess the high-temp regenerator that the 5th mode of the invention described above relates to, refrigerant vapour separates fully with concentrated solution and is derived in high-temp regenerator, therefore becomes Absorption Refrigerator small-sized and that efficient is high.
To achieve these goals, the absorption heat pump that the 7th mode of the present invention relates to, for example shown in Figure 4, possess: absorber 131, it has makes heated medium W flow to inner heated medium stream 131a, absorption liquid Sa absorption refrigeration agent steam Ve, and heat the heated medium W that in heated medium stream 131a, flows, make heated medium W become gas Wv from liquid Wq; Gas-liquid separator 120, it is the gas-liquid separator 120 that any one mode in the cubic formula of first mode to the of the invention described above relates to, it imports fluid Wm, and gas Wv is the heated medium of gas, liquid Wq is the heated medium of liquid, fluid Wm is that this gas-liquid separator separates the heated medium Wv of gas and the heated medium Wq of liquid from the heated medium Wv of the gas of heated medium stream 131a derivation and the mixed fluid of heated medium Wq of liquid; Backflow stream 119B, the heated medium Wq of the liquid that it will separate in gas-liquid separator 120 guides to heated medium stream 131a.
According to such formation, owing to any one mode in the cubic formula of first mode to that possesses the invention described above relates to gas-liquid separator, therefore the heated medium of the heated medium of liquid and gas is separated fully and is derived respectively, becomes absorption heat pump small-sized and that efficient is high.
According to the present invention, owing to possess and comprise the dividing plate that plate-shaped member constitutes, therefore the liquid that has not been separated by baffle plate can be separated by plate-shaped member, also can gas be separated fully with liquid even therefore reduce the size of gas-liquid separator, become gas-liquid separator small-sized and the gas-liquid separation superior performance at the plate-shaped member place.
Description of drawings
Fig. 1 is the skeleton diagram of the formation of the gas-liquid separator that relates to of expression first embodiment of the present invention.Wherein (a) is the longitudinal section of signal, (b) be the B-B of (a) among Fig. 1 to view, be that the C-C of (a) among Fig. 1 is to view (c).
Fig. 2 is the longitudinal section of the high-temp regenerator that relates to of second embodiment of the present invention.
Fig. 3 is the system diagram of the Absorption Refrigerator that relates to of expression the 3rd embodiment of the present invention.
Fig. 4 is the figure of the absorption heat pump that relates to of expression the 4th embodiment of the present invention, and wherein (a) is system diagram, (b) is the fragmentary detail view around the gas-liquid separator.
(a) is the system diagram of absorption heat pump 130A among Fig. 5, and (b) is the part details drawing of the introduction part flow separator 120 on every side of heated medium W among Fig. 5.
Fig. 6 is the horizontal cross of variation of the main part of the gas-liquid separator that relates to of expression first embodiment of the present invention.Wherein (a) is the figure of expression first variation, (b) is the figure of expression second variation, (c) is the figure of expression the 3rd variation.
Fig. 7 is the longitudinal section of signal of the 4th variation of the main part of the gas-liquid separator that relates to of expression first embodiment of the present invention.
Symbol description among the figure: 14... lower header (liquid chamber); 20... gas-liquid separator; 20r... phegma export mouth; 21... baffle plate; 22... dividing plate; 23... peristome; 24... plate-shaped member; 26... liquid level detector; 27... connected entrance; 28... inlet; 28d... fluid-mixing introducing port; 29... downstream chamber; 29e... refrigerant vapour export mouth; 30... Absorption Refrigerator; 31... absorber; 32A... high-temp regenerator; 33... condenser; 34... evaporimeter; 65... control device; 119B... return duct; 120... gas-liquid separator; 130... absorption heat pump; 131a... heated medium pipe; Fm... fluid-mixing; P... cold water (medium is cooled); Sa... concentrated solution (high temperature concentrated solution); Sc... mix concentrated solution; Sw... weak solution; Va... refrigerant vapour (high temperature refrigerant steam); Vb... low-temperature refrigerant steam; Vf... refrigerant liquid; Ve... refrigerant vapour; W... heated medium; Wm... mix heated medium; Wq... heated medium liquid; Wv... heated medium steam.
The specific embodiment
Below, referring to accompanying drawing embodiments of the present invention are described.In addition, for the identical or similar symbol of parts mark identical or suitable in each figure, and the repetitive description thereof will be omitted.
At first referring to Fig. 1, the formation of the gas-liquid separator 20 that first embodiment of the present invention is related to describes.Fig. 1 is the summary pie graph of gas-liquid separator 20.Wherein (a) is the longitudinal section of signal, (b) be the B-B of (a) among Fig. 1 to view, be that the C-C of (a) among Fig. 1 is to view (c).Gas-liquid separator 20 is arranged at (referring to Fig. 2) among the high-temp regenerator 32A typically.
Gas-liquid separator 20, be in the high-temp regenerator 32A of Absorption Refrigerator 30 (referring to Fig. 3) (referring to Fig. 2), produce from the weak solution of heating absorption liquid as the refrigerant vapour Va of gas and the fluid-mixing Fm as the concentrated solution Sa of liquid, the machine that refrigerant vapour Va is separated with concentrated solution Sa.Employed cold-producing medium and solution (absorption liquid) typically, make water as cold-producing medium in Absorption Refrigerator 30 (referring to Fig. 3), use lithium bromide (LiBr) as solution.Concentrated solution Sa is the solution that the amount of cold-producing medium is less than weak solution.Gas-liquid separator 20 possesses: main body 20B, and portion has baffle plate 21 and dividing plate 22 within it; Liquid level detector 26, it detects the liquid level in the main body 20B.
In the upper side of the main body 20B of inlet's 28 sides, be formed with fluid-mixing introducing port 28d as the introducing port that imports fluid-mixing Fm.Fluid-mixing introducing port 28d is formed at upper side, be fluid-mixing Fm and baffle plate 21 collisions that import to main body 20B in order to make, and the fluid-mixing Fm after formation and baffle plate 21 collisions is along the flowing towards the below of the face of baffle plate 21.In the present embodiment, baffle plate 21 constitutes one with dividing plate 22.That is, the top of dividing plate 22 possesses the function as baffle plate 21.Be connected with fluid-mixing pipe 19A at fluid-mixing introducing port 28d.The top board of the main body 20B of 29 sides in the downstream chamber is formed with the refrigerant vapour export mouth 29e as the gas export mouth of deriving refrigerant vapour Va.Refrigerant vapour export mouth 29e also can be formed at the upper side of the main body 20B of downstream chamber's 29 sides, yet, consider from the viewpoint that derives refrigerant vapour Va swimmingly, be preferably the top board that is formed at main body 20B.On refrigerant vapour export mouth 29e, be connected with refrigerant vapour pipe 58.
On the base plate of main body 20B, be formed with concentrated solution export mouth 20n and reflux solution export mouth 20r.Concentrated solution export mouth 20n is the export mouth that the concentrated solution Sa that will separate from fluid-mixing Fm derives to the absorber 31 of Absorption Refrigerator 30 (referring to Fig. 3).Reflux solution export mouth 20r, be the concentrated solution Sa that will from fluid-mixing Fm, separate as reflux solution Sr, the export mouth of deriving to the lower header 14 of high-temp regenerator 32A (referring to Fig. 2).In addition, reflux solution Sr, the difference for the convenience that illustrates according to purposes (supplying with the other side) has been called difference with name, is identical solution with concentrated solution Sa in fact.Concentrated solution export mouth 20n is formed at downstream chamber's 29 sides, and reflux solution export mouth 20r is formed at inlet's 28 sides.Be connected with high temperature concentrated solution pipe 56A at concentrated solution export mouth 20n.20r is connected with return duct 19B at the reflux solution export mouth.
In the bottom of main body 20B, be formed with the connected entrance 27 that is communicated with inlet 28 and downstream chamber 29.In the present embodiment, the dividing plate 22 that extends downwards from the top board of main body 20B does not contact with the base plate of main body 20B, forms connected entrance 27 by between the base plate of the lower end of dividing plate 22 and main body 20B the gap being set.Owing to be formed with connected entrance 27, thereby can on the position that forms concentrated solution export mouth 20n and reflux solution export mouth 20r, have the free degree.If with aperture area is to add up to the mode more than the aperture area that obtains to form connected entrance 27 aperture area of concentrated solution export mouth 20n and the aperture area of reflux solution export mouth 20r, then, be stored in the flowing of concentrated solution Sa of the bottom of main body 20B, mouthful 27 obstructions can not be connected, can make from the derivation of the concentrated solution Sa (Sr) of concentrated solution export mouth 20n and reflux solution export mouth 20r stablely, thereby be fit to.
Part below dividing plate 22 is formed with the connected entrance 23 (referring to (b) among Fig. 1) that is communicated with inlet 28 and downstream chamber 29.Peristome 23 is openings that the fluid-mixing Fm that will import to inlet 28 guides to downstream chamber 29.Peristome 23 typically forms the rectangle (rectangle or square) that has to the limit of vertical direction and horizontal direction extension.Peristome 23, the flow velocity of the big more fluid-mixing Fm that passes through of its area is low more, thereby can improve gas-liquid separation effect.Therefore, as mentioned above, dividing plate 22 is provided on the long as far as possible position of length in the axle vertical direction section that makes main body 20B cylindraceous (can obtain the position of the width of bigger peristome 23).Wishing that peristome 23 is on the other hand big as far as possible, form, for the top performance that makes dividing plate 22 function as baffle plate 21, make the upper end of peristome 23 be positioned at the more below of the lower end of fluid-mixing introducing port 28d, be preferably formed for, between the lower end of the upper end of peristome 23 and fluid-mixing introducing port 28d, guarantee by fluid-mixing Fm along the face of baffle plate 21 downwards flow the distance of separating concentrated solution Sa.For example also can be so that the aluminium Nogata that the upper end of peristome 23 is positioned at dividing plate 22 to half the more mode of below of position of length, form peristome 23.In addition, can also be that the lower end side of peristome 23 extends to the lower end of dividing plate 22, becomes the mode of open communication portion 23 and connected entrance 27.In addition, in the present embodiment, because connected entrance 27 is to form by between the base plate of the lower end of dividing plate 22 and main body 20B the gap being set, even therefore peristome 23 and connected entrance 27 connections also can be known its border, yet under being formed on situation in the dividing plate 22, connected entrance 27 (for example forms under the situation of rectangle at connected entrance 27, the top of connected entrance 27 and two sides or be the state of dividing plate 22 all around), then the border of peristome 23 and connected entrance 27 becomes and is difficult to know.In this case, will till the position of the lower end of plate-shaped member described later, be made as peristome 23, distinguish being made as connected entrance 27 below it.
Top at a plurality of bending plates 24 of being arranged, inaccessible plate 24c is installed, and the fluid-mixing Fm that has been used to prevent to pass through peristome 23 is from breaking away from (not taking a shortcut by the stream of formed crank-like between bending plate 24 fully) to vertical direction between the bending plate 24.Inaccessible plate 24c is rectangular plate-shaped member, and it forms the bending plate 24A that can cover the two ends that are arranged in a plurality of bending plates 24 that set, the length of 24B than the length of length direction.Inaccessible plate 24c is installed in dividing plate 22 in the rectangular mode of face of its face and dividing plate 22.Like this, bending plate 24 just is comprised on the dividing plate 22.
Then referring to Fig. 2, the formation of the high-temp regenerator 32A that second embodiment of the present invention is related to describes.Fig. 2 is the longitudinal section of high-temp regenerator 32A.The high-temp regenerator 32A of present embodiment is tubular regenerator, possesses: Shuo Ming gas-liquid separator 20 before; Lower header 14, it is as the liquid chamber that imports weak solution Sw; A plurality of liquid pipes 10, it makes weak solution Sw flow towards the top; Upper header 15, it is collected in the concentrated solution Sa of generation in the liquid pipe 10 and the fluid-mixing Fm of refrigerant vapour Va as the top endless member; Burner 16, it generates the burning gases that are used for the weak solution Sw in the heating fluid pipe 10 as burner; Outer container 13, it holds these parts.In addition, in liquid pipe 10, be heated concentrated weak solution Sw, strictly, have the situation be mixed with reflux solution Sr (concentrated solution Sa), yet on the meaning of the solution that need to be referred to as regeneration (concentrating), be expressed as weak solution Sw.
On lower header 14, be equipped with a plurality of liquid pipes 10 substantially vertically.So-called liquid pipe 10 is vertical substantially, is meant the vertical substantially state of axle of liquid pipe 10.Substantially vertical being meant, so long as be heated in liquid pipe 10, the refrigerant vapour Va that produces from weak solution Sw evaporation gets final product with the degree that concentrated solution Sa discharges swimmingly.The length of liquid pipe 10, when the height of high-temp regenerator 32A is restricted, then determine can hold the mode in its height, and, synthetically consider to supply with flow, the radical of liquid pipe 10 and the relation between the diameter of the weak solution Sw of high-temp regenerator 32A, because the heat that the weak solution Sw that flows to portion within it provides, and from weak solution Sw, produce refrigerant vapour Va to allow to, and generate concentrated solution Sa, decide.In addition, roughly substantially equally spaced setting many liquid pipes 10 on the concentric circles with lower header 14.Inboard at many liquid pipes 10 that roughly substantially equally spaced set on the concentric circles with lower header 14 is formed with combustion chamber 18, is used for combustion fuel to generate burning gases.
At the top of many liquid pipes 10, be connected with upper header 15.Upper header 15, same with lower header 14, typically form, horizontal profile is circular, vertical section is rectangular-shaped.On upper header 15, be connected with fluid-mixing pipe 19A, be used for the fluid-mixing Fm of concentrated solution Sa and refrigerant vapour Va is guided to gas-liquid separator 20.Fluid-mixing pipe 19A also can be connected the side of upper header 15.In the formed hollow sectors of the central part of upper header 15, be equipped with burner 16.In addition, upper header 15 is connected by communicating pipe 11 with lower header 14, and sets the have liquid level sensor liquid level test section 12 of (not shown) on communicating pipe 11, in the mode of the liquid level that can control liquid pipe 10 and constitute.
Then referring to Fig. 3, the formation of the Absorption Refrigerator 30 that the 3rd embodiment of the present invention is related to describes.Fig. 3 is the system diagram of Absorption Refrigerator 30.Absorption Refrigerator 30 is double-effect absorption refrigerating machine, possesses: evaporimeter 34, and it makes refrigerant liquid Vf evaporation produce refrigerant vapour Ve and cools off cold water p by utilizing the heat as the cold water p of the medium that is cooled; Absorber 31, the refrigerant vapour Ve that it will produce in evaporimeter utilize mixing concentrated solution Sc to absorb; High-temp regenerator 32A, its will be in absorber 31 absorption refrigeration agent steam Ve concentration is reduced and the weak solution Sw that obtains imports, heat dilute solution Sw makes the cold-producing medium evaporation, the concentrated solution that generates the concentration rising is that high temperature concentrated solution Sa is (in order to distinguish with the low temperature concentrated solution Sb that is generated by low-temperature regenerator 32B, sometimes the concentrated solution Sa that also will be generated by high-temp regenerator 32A is called " high temperature concentrated solution Sa "); Low-temperature regenerator 32B, similarly, it will import the weak solution Sw after concentration reduces by absorption refrigeration agent steam Ve in absorber 31, and heat dilute solution Sw makes the cold-producing medium evaporation, generates the low temperature concentrated solution Sb that concentration rises; Condenser 33, it condenses the low-temperature refrigerant steam Vb cooling of evaporating from weak solution Sw in low-temperature regenerator 32B, generate the refrigerant liquid Vf that delivers to evaporimeter 34; Control device 65, the running of its control Absorption Refrigerator 30.Employed cold-producing medium and solution in Absorption Refrigerator 30, typically, make water as mentioned above, use lithium bromide (LiBr) as solution as cold-producing medium, yet be not limited to this, also can use with other cold-producing medium, the combination of solution (absorbent).
In evaporimeter 34, be equipped with cold water pipe 34a, be used for mobile cold water p as the object that will cool off.Cold water pipe 34a utilizes machine (not shown) to be connected by pipe arrangement 52 with the cold water of air processor etc.In addition, in evaporimeter 34, above cold water pipe 34a, be equipped with refrigerant liquid spreading nozzle 34b, be used for scattering refrigerant liquid Vf to cold water pipe 34a.In the bottom of evaporimeter 34, be formed with the 34c of storage portion, be used to store the refrigerant liquid Vf that is imported.
In absorber 31, be equipped with the cooling water pipe 31a of the cooling water q that flows in inside, this cooling water q, the absorption heat that produces when being used to be absorbed in the mixed solution Sc absorption refrigeration agent steam Ve that mixes with high temperature concentrated solution Sa and low temperature concentrated solution Sb.Cooling water pipe 31a is connected by the cooling water pipe 33a in pipe arrangement 53 and the condenser 33 respectively, and passes through pipe arrangement 54 and be connected with cooling tower (not shown).In addition, in absorber 31, above cooling water pipe 31a, be equipped with concentrated solution spreading nozzle 31b, be used for scattering mixing concentrated solution Sc to cooling water pipe 31a.Absorber 31 below cooling water pipe 31a, is formed with the 31c of storage portion, is used to store absorption refrigeration agent steam Ve and weak solution Sw that concentration has been reduced.
In the bottom of absorber 31, be connected with weak solution pipe 55, be used for the weak solution Sw of the 31c of storage portion is guided to high-temp regenerator 32A and low-temperature regenerator 32B.On weak solution pipe 55, be equipped with solution pump 38, be used for weak solution Sw is pressed and delivered to two regenerator 32A, 32B.Solution pump 38 typically constitutes, and can pass through inverter (not shown) and regulate rotary speed, and constitute, can pressurized delivered and the weak solution Sw of the corresponding flow of cooling load.On the weak solution pipe 55 in the downstream of solution pump 38, be equipped with at weak solution Sw and mix the cryogenic fluid heat exchanger 36 that carries out heat exchange between the concentrated solution Sc.On cryogenic fluid heat exchanger 36, being connected with again flows mixes the concentrated solution pipe 56 of concentrated solution Sc.Cryogenic fluid heat exchanger 36, though use plate-type exchanger typically, also can be shell-tube type or other heat exchanger.
Weak solution pipe 55, the downstream at cryogenic fluid heat exchanger 36 branches into: the weak solution pipe 55A that is connected with high-temp regenerator 32A, with the weak solution pipe 55B that is connected with low-temperature regenerator 32B.On weak solution pipe 55A, be equipped with the high-temperature solution heat exchanger 35 that between weak solution Sw and high temperature concentrated solution Sa, carries out heat exchange.On high-temperature solution heat exchanger 35, be connected with the high temperature concentrated solution pipe 56A of the high temperature concentrated solution Sa that flows again.High-temperature solution heat exchanger 35, though use plate-type exchanger typically, also can be shell-tube type or other heat exchanger.
Weak solution pipe 55A, 32A is connected with high-temp regenerator.On high-temp regenerator 32A, be connected with high temperature concentrated solution pipe 56A.In addition, on high-temp regenerator 32A, be connected with refrigerant vapour pipe 58, the refrigerant vapour that is produced that is used to flow is high temperature refrigerant steam Va (in order to distinguish with the low-temperature refrigerant steam Vb that is generated by low-temperature regenerator 32B, also will being called " high temperature refrigerant steam Va " by the refrigerant vapour Va that high-temp regenerator 32A is generated sometimes).
On low-temperature regenerator 32B, be equipped with heating steam pipe 32Ba, be used for mobile as the high temperature refrigerant steam Va that is used for the heating source of heat dilute solution Sw.Heating steam pipe 32Ba, an end is connected in refrigerant vapour pipe 58.The other end is connected in the refrigerant pipe 59 that condenses.The refrigerant pipe 59 that condenses is high temperature refrigerant steam Va to be condensed in heating steam pipe 32Ba and the refrigerant liquid Vd that forms guides to the pipe arrangement of condenser 33.In low-temperature regenerator 32B, be equipped with weak solution spreading nozzle 32Bb, be used for scattering the weak solution Sw that is imported to heating steam pipe 32Ba.Weak solution spreading nozzle 32Bb, 55B is connected with the weak solution pipe.
In condenser 33, be equipped with the cooling water pipe 33a of the cooling water q that flows, this cooling water q is used for cooling off the low-temperature refrigerant steam Vb that produces at low-temperature regenerator 32B.Cooling water pipe 33a, an end is connected by the cooling water pipe 31a in pipe arrangement 53 and the absorber 31, and the other end passes through pipe arrangement 54 and is connected with cooling tower (not shown).
In the bottom of low-temperature regenerator 32B, be connected with the low temperature concentrated solution pipe 56B that the low temperature concentrated solution Sb after concentration rises is passed through.High temperature concentrated solution pipe 56A and low temperature concentrated solution pipe 56B are formed by connecting and are concentrated solution pipe 56.Concentrated solution pipe 56, via cryogenic fluid heat exchanger 36,31b is connected with the concentrated solution spreading nozzle.In the bottom of condenser 33, be connected with the refrigerant liquid pipe 60 of deriving refrigerant liquid Vf to evaporimeter 34.Refrigerant liquid Vf is the refrigerant liquid that has mixed refrigerant liquid Vc and refrigerant liquid Vd, and wherein: refrigerant liquid Vc is, low-temperature refrigerant steam Vb condenses and the refrigerant liquid that forms; Refrigerant liquid Vd is that high temperature refrigerant steam Va condenses in heating steam pipe 32Ba, and the refrigerant liquid that is cooled in condenser 33.
Continuation is with reference to Fig. 1～Fig. 3, to the effect of gas-liquid separator 20 and high-temp regenerator 32A, describes with the effect of Absorption Refrigerator 30.At first, referring to Fig. 3, the circulation of the refrigerant side of Absorption Refrigerator 30 is described.In condenser 33, be received in the low-temperature refrigerant steam Vb that evaporates among the low-temperature regenerator 32B, and use the cooling water q that supplies with by cooling tower (not shown), in cooling water pipe 33a, flow to cool off to condense, form refrigerant liquid Vc.The refrigerant liquid Vc that condenses and obtain mixes with refrigerant liquid Vd and to be refrigerant liquid Vf, and is transported to evaporimeter 34, is stored among the 34c of storage portion as refrigerant liquid Vf.Be stored in the refrigerant liquid Vf among the 34c of storage portion, be transported to refrigerant liquid spreading nozzle 34b by refrigerated medium pump 39.When the refrigerant liquid Vf of evaporimeter 34 when refrigerant liquid spreading nozzle 34b spreads to cold water pipe 34a, refrigerant liquid Vf accepts to evaporate from the heat of the cold water p in the cold water pipe 34a on the one hand, cold water p is cooled.The cold water p that is cooled is sent to and utilizes cold and hot place (not shown) to use.On the other hand, the refrigerant liquid Vf of evaporation becomes refrigerant vapour Ve in evaporimeter 34, moves to the absorber 31 that is communicated with.
The circulation of the solution side of Absorption Refrigerator 30 then, is described.In absorber 31, from the solution S c of concentrated solution spreading nozzle 31b distribution high concentration, solution S c is absorbed in the refrigerant vapour Ve that produces in the evaporimeter 34 and becomes weak solution Sw.Weak solution Sw is stored in the 31c of storage portion.The absorption heat that solution S c produces when absorption refrigeration agent steam Ve is removed by the cooling water q that flows in cooling water pipe 31a.The weak solution Sw of the 31c of storage portion, by solution pump 38 respectively to high-temp regenerator 32A and low-temperature regenerator 32B pressurized delivered.In addition, also can constitute, make the solution circulation that is stored among the 31c of storage portion, spread to cooling water pipe 31a by solution circulation pump (not shown).Like this, can soak cooling water pipe 31a fully by enough solution, and can prevent to contact the solution secund of cooling water pipe 31a.In addition, can also constitute, with solution pump 38 double as solution circulation pumps.In this case, can branch out pipe arrangement, be connected to concentrated solution spreading nozzle 31b from the weak solution pipe 55 between solution pump 38 and the low temperature heat exchanger 36.
The weak solution Sw that in weak solution pipe 55, flows, at first in cryogenic fluid heat exchanger 36 with mix concentrated solution Sc and carry out heat exchange, and after recuperation of heat, shunt, a part flows in weak solution pipe 55A and to high-temperature solution heat exchanger 35 guiding, remaining flows in weak solution pipe 55B and guides to low-temperature regenerator 32B.In weak solution pipe 55A, flow and flow into the weak solution Sw of high-temperature heat exchanger 35, carry out heat exchange, and after temperature rises, in weak solution pipe 55A, flow and be imported into high-temp regenerator 32A with the high temperature concentrated solution Sa that derives from high-temp regenerator 32A.
At this,, the effect of high-temp regenerator 32A and gas-liquid separator 20 is described referring to Fig. 2 and Fig. 1.In weak solution pipe 55A, flow and be directed to the weak solution Sw of high-temp regenerator 32A, flow into lower header 14.Flow into the weak solution Sw of lower header 14, arrive the bottom of each liquid pipe 10, and the pressure by solution pump 38 (referring to Fig. 3), in a plurality of liquid pipes 10, rise and flow to upper header 15.Weak solution Sw, in the process that in each liquid pipe 10, rises, burned gas Gb heating, cold-producing medium evaporates and produces refrigerant vapour Va, and the concentration of solution itself rises and becomes concentrated solution Sa.At this moment, the liquid level of regulating each liquid pipe 10 by solution pump 48 (referring to Fig. 3), being below upper header 15, and above the minimum altitude of regulation.The minimum altitude of regulation is the damage of the liquid pipe 10 that causes for heating under the state that prevents from not have fluid in liquid pipe 10, and should be full of the minimum altitude of solution in advance in liquid pipe 10.In addition, the liquid level of each liquid pipe 10 is set in the below of upper header 15, is in order to prevent to produce following situation: when the liquid level of certain liquid pipe 10 arrived upper header 15, solution flowed on the top of liquid pipe 10 (upper header 15), and, the phenomenon that solution descends in other liquid pipe 10.The mode that refrigerant vapour Va mixes the fluid-mixing Fm that forms with the concentrated solution Sa that obtains with weak solution Sw concentration is risen flow into upper header 15 and is collected from each liquid pipe 10, and by fluid-mixing pipe 19A inflow gas-liquid separator 20.
Flow into the fluid-mixing Fm of gas-liquid separator 20,28d flow into inlet 28 from the fluid-mixing introducing port.Flow into the fluid-mixing Fm of inlet 28, with baffle plate 21 collisions that are in the flow direction front, thereby its flow direction is changed.In the present embodiment, because baffle plate 21 constitutes with dividing plate 22 one, therefore also can be considered as the top collision of fluid-mixing Fm and dividing plate 22.When the fluid-mixing Fm of refrigerant vapour Va and concentrated solution Sa collides baffle plate 21 and during the direction that change to flow, the piece of bigger concentrated solution Sa is separated from fluid-mixing Fm, separated concentrated solution Sa falls and is stored in the bottom of main body 20B.Be stored in the concentrated solution Sa of the bottom of main body 20B, also flow into downstream chamber 29 by connected entrance 27.In addition, because the concentrated solution Sa that separates from fluid-mixing Fm falls, sometimes the liquid level of concentrated solution Sa of bottom that is stored in inlet's 28 sides of main body 20B can be disorderly, yet, utilize liquid level detector 26, the dividing plate 22 of the involved bending plate 24 of liquid level of maintenance concentrated solution Sa blocks the state of (be positioned in the present embodiment than the lower end of dividing plate 22 and more lean on top), and the dividing plate 22 that therefore comprises bending plate 24 plays the effect of breakwater, and the liquid level of the concentrated solution Sa of downstream chamber's 29 sides is not disorderly and stable.
Collide the separated and remaining refrigerant vapour Va of baffle plate 21 concentrated solution Sa by fluid-mixing Fm, mainly flow downwards, and relative with the liquid level of the concentrated solution Sa of the bottom that is stored in main body 20B and be blocked the outlet, thereby direction changes to peristome 23 sides.In flowing into the refrigerant vapour Va of peristome 23, contain drop by the concentrated solution Sa not separated with the collision of baffle plate 21.Flow into the refrigerant vapour Va of the drop that contains concentrated solution Sa of peristome 23, flow into the stream of formed crank-like between a plurality of bending plates 24.The refrigerant vapour Va that contains the drop of concentrated solution Sa, between bending plate 24 in the formed crank-like stream, face along bending plate 24, when in downstream chamber 29, flowing, part on the mountain of " く " word (paddy) changes the direction that flows, at this moment, the drop of concentrated solution Sa is separated from refrigerant vapour Va.In the present embodiment, since from the manufacturing cost that suppresses bending plate 24 viewpoint consider, bending plate 24 is bent into " く " font (1 crest line), therefore contain the flow direction of refrigerant vapour Va of the drop of concentrated solution Sa, between bending plate 24, change once in the stream of formed crank-like.
Owing to bending plate 24 sets for roughly vertical mode with its crest line, so, the drop of refrigerant vapour Va mobile and separated concentrated solution Sa on the stream of formed crank-like between the bending plate 24 of the drop by containing concentrated solution Sa is because the work of gravity falls in order to the mode that the face along bending plate 24 slides.Like this, can improve the effect that the drop of concentrated solution Sa separates from refrigerant vapour Va.The drop of the concentrated solution Sa that falls is stored in the bottom of downstream chamber's 29 sides.Be stored in the concentrated solution Sa of bottom, become one with the concentrated solution Sa that is stored in inlet's 28 sides by connected entrance 27.In addition, the aperture area of peristome 23 is big more, then can make the flow velocity of refrigerant vapour Va of the drop that contains concentrated solution Sa that flow into peristome 23 low more, can improve gas-liquid separation effect.
The refrigerant vapour Va that between bending plate 24, flows out the stream of formed crank-like, be directed to downstream chamber's 29 sides main body 20B sidewall and the direction that flows changed into upward.At this moment, under the situation of the drop that also contains concentrated solution Sa in refrigerant vapour Va, by the collision of refrigerant vapour Va to sidewall, the drop of concentrated solution Sa is separated and be stored in the bottom of main body 20B.Concentrated solution Sa in the bottom storage of main body 20B, mainly derived and flowed to absorber 31 (referring to Fig. 3) from concentrated solution export mouth 20n, remainder is derived from reflux solution export mouth 20r as reflux solution Sr, and is back to lower header 14 by concentrated solution return duct 19B.In the present embodiment, because concentrated solution export mouth 20n is formed at downstream chamber's 29 sides, therefore can stably take out concentrated solution Sa from downstream chamber's 29 sides of liquid level stabilizing.In addition, also can form concentrated solution export mouth 20n in inlet's 28 sides according to the amount of the Sa of the concentrated solution of taking out and the liquid level situation of inlet's 28 sides, 29 sides form reflux solution export mouth 20r in the downstream chamber, and go out concentrated solution Sa from inlet's 28 side-draws.In addition, also concentrated solution export mouth 20n and reflux solution export mouth 20r both sides can be formed at below the dividing plate 22 between inlet's 28 sides and downstream chamber's 29 sides (boundary member) side by side.Like this, just the both sides of concentrated solution Sa and reflux solution Sr can be taken out from same liquid level situation.Perhaps, also can be with the both sides of concentrated solution export mouth 20n and reflux solution export mouth 20r, be formed at either party of inlet's 28 sides or downstream chamber's 29 sides.These can consider that the capacity of high-temp regenerator 32A and the size of gas-liquid separator 20 etc. decide.On the other hand, refrigerant vapour Va is derived from refrigerant vapour export mouth 29e, and flows to low-temperature regenerator 32B (referring to Fig. 3) in refrigerant vapour pipe 58.
Get back to Fig. 3 once more, continue the explanation of the circulation of solution side.The high temperature concentrated solution Sa that derives and flow in high temperature concentrated solution pipe 56A from high-temp regenerator 32A is directed to high-temperature solution heat exchanger 35, and carries out heat exchange with the weak solution Sw that flows to high-temp regenerator 32A, and temperature is reduced.On the other hand, the high temperature refrigerant steam Va that from high-temp regenerator 32A, derives and in refrigerant vapour pipe 58, flow, the heating steam pipe 32Ba of inflow low-temperature regenerator 32B.
On the other hand, flow in weak solution pipe 55B and be directed to the weak solution Sw of low-temperature regenerator 32B, 32Bb is scattered from the weak solution spreading nozzle.From the weak solution Sw that weak solution spreading nozzle 32Bb is scattered, be heated the high temperature refrigerant steam Va heating of flowing among the steam pipe 32Ba, the cold-producing medium evaporation among the weak solution Sw in the low-temperature regenerator 32B becomes low temperature concentrated solution Sb.On the other hand, carry to condenser 33 as low-temperature refrigerant steam Vb from the cold-producing medium of weak solution Sw evaporation.The low temperature concentrated solution Sb that temperature rises owing to accept from the heat of high temperature refrigerant steam Va is because of the pressure in gravity and the low-temperature regenerator 32B is derived to low temperature concentrated solution pipe 56B.In addition, the high temperature refrigerant steam Va that flows in heating steam pipe 32Ba is absorbed heat by weak solution Sw and condenses and become refrigerant liquid Vd, and flows in the refrigerant pipe 59 that condenses and be directed to condenser 33.
The low temperature concentrated solution Sb that from low-temperature regenerator 32B, derives and in low temperature concentrated solution pipe 56B, flow, with the high temperature concentrated solution Sa interflow of from high-temperature solution heat exchanger 35, deriving and in high temperature concentrated solution pipe 56A, flowing and, become and mix concentrated solution Sc and in concentrated solution pipe 56, flow.Afterwards, mix concentrated solution Sc and flow into cryogenic fluid heat exchanger 36, carry out heat exchange, temperature is reduced with the weak solution Sw that from absorber 31, derives.The lowered mixing concentrated solution of temperature Sc is directed to absorber 31, and scatters to cooling water pipe 31a from concentrated solution spreading nozzle 31b.After, repeat same circulation.
In the above description, establish liquid level detector 26 is arranged at level control with in the container 25, yet also can be arranged in the main body 20B.In this case, be preferably,, hang mode down, the high liquid level test bar 26H that detects high liquid level is set and detects the low liquid level test bar 26L that hangs down liquid level with top board from main body 20B in disorderly less downstream chamber's 29 sides of the liquid level of concentrated solution Sa.Like this, do not need level control can suppress manufacturing cost with container 25.Yet,, be preferably disposed on level control with in the container 25 for fear of the influence of the heat that is subjected to refrigerant vapour Va.In addition, establish liquid level detector 26 and be electrode bar, yet, also can for example be electrode bar liquid level detectors in addition such as float switch.
Then referring to Fig. 4, the formation of the absorption heat pump 130 that the 4th embodiment of the present invention is related to describes.(a) is the system diagram of absorption heat pump 130 among Fig. 4, and (b) is the fragmentary detail view around the gas-liquid separator 120 among Fig. 4.Absorption heat pump 130, the absorption heat pump of single-stage typically.Absorption heat pump 130 possesses: absorber 131, and it utilizes concentrated solution Sa to be absorbed in the cold-producing medium Ve of evaporation in the evaporimeter 134; Regenerator 132, it imports weak solution Sw and produces refrigerant vapour Vb by heating from absorber 131; Condenser 133, its refrigerant vapour Vb that will produce in regenerator 132 cools off, and it is condensed and obtains refrigerant liquid Vf; Evaporimeter 134, it imports refrigerant liquid Vf from condenser 133, makes its evaporation produce refrigerant vapour Ve; Gas-liquid separator 120, the heated medium W that it will heat in absorber 131, import as mixing heated medium Wm, and this mixing heated medium Wm is as the heated medium steam Wv of the heated medium of gas with as the mixed fluid of heated medium liquid Wq of the heated medium of liquid, and gas-liquid separator 120 is separated into heated medium steam Wv and heated medium liquid Wq with it.In addition, when not considering the concentration of each solution (weak solution Sw and concentrated solution Sa), general designation also is called " absorption liquid S " or " solution S " simply in the following description.Absorption liquid S in the present embodiment (mixture of absorbent and cold-producing medium) uses the LiBr aqueous solution.In addition, the general name that heated medium W is heated medium liquid Wq, heated medium steam Wv, mix heated medium Wm.
Regenerator 132 has regenerated heat source capsule 132a that constitutes regenerated heat medium stream and the weak solution spreading nozzle 132b that scatters weak solution Sw.As the thermal medium h that is used to heat concentrating dilute solution Sw, typically, flow into warm water to regenerated heat source capsule 132a, yet, also can will discharge gas or exhaust steam etc. as thermal medium.In the bottom of regenerator 132, be formed with the 132c of storage portion, be used for storing cold-producing medium evaporation (cold-producing medium that will evaporate is called refrigerant vapour Vb) concentration rising afterwards of the weak solution Sw that is scattered and the concentrated solution Sa that obtains.The concentrated solution spreading nozzle 131b of the 132c of storage portion of regenerator 132 and absorber 131, solution pipe arrangement 155 by the concentrated solution Sa that flows connects, the 131c of storage portion of the weak solution spreading nozzle 132b of regenerator 132 and absorber 131, the solution pipe arrangement 156 by the weak solution Sw that flows connects.On solution pipe arrangement 155, be equipped with solution pump 138, be used for the concentrated solution Sa of regenerator 132 is pressed and delivered to absorber 131.Solution pump 138 constitutes, has the inverter 138x that is connected with weak solution liquid level detector 168 usefulness signal cables, and can regulate rotary speed according to weak solution liquid level detector 168 detected liquid levels, thereby regulate the flow of the concentrated solution Sa that is pressed and delivered to absorber 131.In addition, on solution pipe arrangement 155 and solution pipe arrangement 156, be equipped with the solution heat exchanger 136 that is used between weak solution Sw and concentrated solution Sa, carrying out heat exchange.Solution heat exchanger 136, however use plate-type exchanger also can use shell-tube type or other heat exchanger typically.Regenerator 132 constitutes, and can pass through solution pipe arrangement 156, will be in absorber 131 absorption refrigeration agent steam Ve concentration is reduced and the weak solution Sw that obtains imports, utilize the heat of thermal medium h to make the cold-producing medium evaporation, be regenerated as the concentrated solution Sa of high concentration.
Shown in (b) among Fig. 4, gas-liquid separator 120 is except that following point, identical with the formation of gas-liquid separator 20 (referring to Fig. 1).Gas-liquid separator 120 is with the difference of gas-liquid separator 20 (referring to Fig. 1): save level control with container 25 (referring to Fig. 1) and 25u of last communicating pipe (referring to Fig. 1) and lower communicating tube 25w (referring to Fig. 1), liquid level detector 26 is arranged in the downstream chamber 29; Substitute the fluid-mixing pipe 19A (referring to Fig. 1) that is used to import fluid-mixing Fm (referring to Fig. 1), be provided with the mixing heated medium pipe 119A that is used to import mixing heated medium Wm; In the bottom of main body 20B is not to store high temperature concentrated solution Sa (referring to Fig. 1) but storage heated medium liquid Wq; Substitute the return duct 19B (referring to Fig. 1) be used to derive reflux solution Sr (referring to Fig. 1), be provided with the return duct 119B of the backflow stream that is configured for deriving heated medium liquid Wq; Saved high temperature concentrated solution pipe 56A (referring to Fig. 1); Substitute the refrigerant vapour pipe 58 (referring to Fig. 1) that is used to derive high temperature refrigerant steam Va (referring to Fig. 1), be provided with the heated medium steam pipe 158 that is used to derive heated medium steam Wv; In the bottom of gas-liquid separator 120, be connected with the additional heated medium pipe 141 that is used to import additional heated medium Ws, and should be used in gas-liquid separator 120, replenishing heated medium W by additional heated medium Ws.Gas-liquid separator 120, identical with the formation of gas-liquid separator 20 (referring to Fig. 1) except that above-mentioned point, in this detailed (as required with reference to gas-liquid separator 20 (referring to Fig. 1) explanation).
Mix heated medium pipe 119A and constitute, be connected, can will mix heated medium Wm from absorber 131 and import to inlet 28 with the end of the heated medium pipe 131a of absorber 131.Return duct 119B constitutes, and is connected with the other end of the heated medium pipe 131a of absorber 131, the heated medium liquid Wq that separates in gas-liquid separator 120 can be supplied to heated medium pipe 131a.On return duct 119B, be equipped with heated medium liquid pump 118, the heated medium liquid Wq that is used for separating at gas-liquid separator 120 is pressed and delivered to heated medium pipe 131a.Replenish heated medium pipe 141, be provided with following purpose, promptly, in order to replenish, replenish heated medium Ws and outside system, import owing to derive heated medium steam Wv heated medium W that reduce, circulation between gas-liquid separator 120 and absorber 131 from gas-liquid separator 120.On additional heated medium pipe 141, have along the arranged in order of the flow direction that replenishes heated medium Ws: replenish heated medium pump 142, be used for additional heated medium Ws is supplied to gas-liquid separator 120; Heat exchanger 143 is used for warm water k preheating and replenishes heated medium Ws; Heat exchanger 144 is used for weak solution Sw preheating and replenishes heated medium Ws.Heat exchanger 144 connects than solution heat exchanger 136 and more leans on the solution pipe arrangement 156 of upstream side, thereby can import weak solution Sw.In addition, in the drawings, for convenience, represented to replenish the situation that heated medium pipe 141 is connected to the downstream chamber 29 of gas-liquid separator 120, yet, the preferred downstream chamber 29 that is connected to gas-liquid separator 120 that substitutes, the inlet 28 that heated medium pipe 141 is connected to gas-liquid separator 120 will be replenished, perhaps substitute and be connected to gas-liquid separator 120, also can be connected to the suction side of heated medium liquid pump 118 or the return duct 119B of ejection side, or heated medium pipe 131a.Like this, can suppress to follow and replenish the liquid level disorder that sets part (downstream chamber 29 in the present embodiment) that heated medium Ws flows into the liquid level detector 26 of gas-liquid separator 120, can realize stable liquid level control.Be connected under the situation of downstream chamber 29 of gas-liquid separator 120 will replenishing heated medium pipe 141, shown in (a) among Fig. 1, can be provided with the level control of main body 20B split with container 25, set liquid level detector 26 in level control in container 25.In addition, be connected under the situation of gas-liquid separator 120 will replenishing heated medium pipe 141, if be connected with gas-liquid separator 120 than the position below more, the lower end of low liquid level test bar 26L, then can supply in the heated medium liquid Wq that is stored in the gas-liquid separator 120, and reduce the phenomenon of the liquid level disorder that in gas-liquid separator 120, makes heated medium liquid Wq formation replenishing heated medium Ws.Supply to the additional heated medium liquid Ws in the gas-liquid separator 120 in addition, usually low than the heated medium liquid Wq temperature that is stored in the gas-liquid separator 120, yet by will replenish heated medium pipe 141 than the lower end of low liquid level test bar 26L more below the position be connected to gas-liquid separator 120, the additional heated medium Ws of lower temperature can directly not impact the component parts of gas-liquid separator 120, component parts at gas-liquid separator 120 can not produce temperature shock, can prolong the life expectancy of gas-liquid separator 120.
The circulation of the refrigerant side of above-mentioned such absorption heat pump that constitutes 130 at first is described, in condenser 133, be received in the regenerator 132 the refrigerant vapour Vb of evaporation, and use the cooling water q that supplies with from cooling tower (not shown), among cooling water pipe 133a, flow that its cooling is condensed to become refrigerant liquid Vf.The refrigerant liquid Vf that has condensed is transported to evaporimeter 134 by refrigerated medium pump 139, is stored in the 134c of storage portion.At this moment, utilize 169 pairs of flow control valves 166 of refrigerant liquid bit detector to regulate, so that when the liquid level of the 134c of storage portion of evaporimeter 134 is low, enlarge its aperture, and under the high situation of liquid level, reduce its aperture.Be stored in the refrigerant liquid Vf in the evaporimeter 134, p heats by thermal medium, becomes refrigerant vapour Ve.At this moment, in the evaporimeter 134, become because the pressure of the degree that the heat refrigerant liquid Vf of warm water evaporates.Refrigerant liquid Vf evaporates and the refrigerant vapour Ve of generation in evaporimeter 134, moves to the absorber 131 that is communicated with.
The circulation of the solution side of absorption heat pump 130 then, is described.In absorber 131, concentrated solution Sa scatters from concentrated solution spreading nozzle 131b, and concentrated solution Sa is absorbed in the refrigerant vapour Ve that produces in the evaporimeter 134 and becomes weak solution Sw.In absorber 131, when concentrated solution Sa absorption refrigeration agent steam Ve, produce absorption heat.Absorb heat by this, the heated medium liquid Wq that flows in heated medium pipe 131a is heated, and one of them part evaporation and become steam.At this, the effect around the gas-liquid separator 120 that is used to take out heated medium steam Wv is described.
Gas-liquid separator 120 as mentioned above, stores heated medium liquid Wq in the bottom, by replenishing heated medium pipe 141, import outside system and replenish heated medium Ws, up to the liquid level of heated medium liquid Wq for regulation.Replenish heated medium Ws, according to liquid level by the heated medium liquid Wq in the detected main body 20B of liquid level detector 26, be pressed and delivered to the additional heated medium pump 142 that rotary speed is conditioned, temperature rises at every turn by heat exchanger 143 and heat exchanger 144 time, and flow into gas-liquid separator 120.Be stored in the heated medium liquid Wq of the bottom of main body 20B, derived, and flow into heated medium pipe 131a by return duct 119B from export mouth 20r.Heated medium liquid Wq, when flowing in heated medium pipe 131a, because the absorption heat that produces when concentrated solution Sa absorption refrigeration agent steam Ve is heated, one of them part evaporation becomes heated medium steam Wv.The part of heated medium liquid Wq is evaporated and the heated medium steam Wv of generation, mix heated medium Wm with heated medium liquid Wq conduct, derive from heated medium pipe 131a, and flow into gas-liquid separator 120 by mixing heated medium pipe 119A.
Flow into the mixing heated medium Wm of gas-liquid separator 120,28d flow into inlet 28 from the fluid-mixing introducing port.Flow into the mixing heated medium Wm of inlet 28, collide the baffle plate 21 that is present in its flow direction front and change its flow direction.In the present embodiment, because baffle plate 21 constitutes with dividing plate 22 one, therefore also can be considered as mixing the top collision of heated medium Wm and dividing plate 22.When the mixing heated medium Wm of heated medium steam Wv and heated medium liquid Wq collides baffle plate 21 and during the direction that change to flow, heated medium liquid Wq is separated from mix heated medium Wm, separated heated medium liquid Wq falls, and is stored in the bottom of main body 20B.Be stored in the heated medium liquid Wq of the bottom of main body 20B, also flow into downstream chamber 29 by connected entrance 27.In addition, because the heated medium liquid Wq that separates from mix heated medium Wm falls, sometimes the liquid level of heated medium liquid Wq of bottom that is stored in inlet's 28 sides of main body 20B can be disorderly, yet, utilize liquid level detector 26, the dividing plate 22 of the involved bending plate 24 of liquid level of maintenance heated medium liquid Wq blocks the state of (be positioned at than the lower end of dividing plate 22 and more lean on top) in the present embodiment, therefore the dividing plate 22 that comprises bending plate 24 plays the effect of breakwater, and the liquid level of the concentrated solution Sa of downstream chamber's 29 sides is not disorderly and stable.
Collide baffle plate 21 by mixing heated medium Wm, the heated medium steam Wv that heated medium liquid Wq is separated and remaining, mainly flow downwards, and relative with the liquid level of the heated medium liquid Wq of the bottom that is stored in main body 20B and be blocked the outlet, thereby direction changes to peristome 23 sides.In flowing into the heated medium steam Wv of peristome 23, contain drop by the heated medium liquid Wq not separated with the collision of baffle plate 21.Flow into the heated medium steam Wv of the drop that contains heated medium liquid Wq of peristome 23, flow into the stream of formed crank-like between a plurality of bending plates 24.The heated medium steam Wv that contains the drop of heated medium liquid Wq, between bending plate 24 in the formed crank-like stream, face along bending plate 24, when in downstream chamber 29, flowing, part on the mountain of " く " word (paddy) changes the direction that flows, at this moment, the drop of heated medium liquid Wq is separated from heated medium steam Wv.
Owing to bending plate 24 sets in the roughly vertical mode of its crest line, so, the heated medium steam Wv of the drop by containing heated medium liquid Wq drop of mobile and separated heated medium liquid Wq in the formed crank-like stream between bending plate 24 is because the work of gravity falls in order to the mode that the face along bending plate 24 slides.Like this, can improve the effect that the drop of heated medium liquid Wq separates from heated medium steam Wv.The drop of the heated medium liquid Wq that falls is stored in the bottom of downstream chamber's 29 sides.Be stored in the heated medium liquid Wq of bottom, become one with the heated medium liquid Wq that is stored in inlet's 28 sides by connected entrance 27.In addition, the aperture area of peristome 23 is big more, then can make the flow velocity of the heated medium steam Wv that contains heated medium liquid Wq drop that flow into peristome 23 low more, can improve gas-liquid separation effect.
The heated medium steam Wv that between bending plate 24, flows out the formed crank-like stream, be directed to downstream chamber's 29 sides main body 20B sidewall and the direction that flows changed into upward.At this moment, under the situation of the drop that also contains heated medium liquid Wq in heated medium steam Wv, by the collision of heated medium steam Wv to sidewall, the drop of heated medium liquid Wq is separated, and is stored in the bottom of main body 20B.Afterwards, heated medium steam Wv is derived from export mouth 29e, and is fed into the place that utilizes steam by heated medium steam pipe 158.Like this, in the present embodiment,,, the power of pump is reduced because at supplying with the flow that heat can reduce thermal medium owing to can take out specific enthalpy (enthalpy) greater than the steam of liquid and supply to the steam utilization place.
Return the explanation of circulation of the solution side of absorption heat pump 130.Absorption refrigeration agent steam Ve reduces concentration and the weak solution Sw that obtains in absorber 131, is stored in the 131c of storage portion.The weak solution Sw of the 131c of storage portion is sent to regenerator 132 owing to gravity reaches interior pressure reduction.Weak solution Sw arrives the way of regenerators 132 from absorber 131, and in heat exchanger 144, carry out heat exchange and temperature is reduced with additional heated medium Ws, and, in solution heat exchanger 136, carry out heat exchange and temperature is reduced with concentrated solution Sa.Be sent to the weak solution Sw of regenerator 132, scatter from weak solution spreading nozzle 132b.From the weak solution Sw of weak solution spreading nozzle 132b distribution, the thermal medium h heating of in regenerated heat source capsule 132a, being flowed, the cold-producing medium among the weak solution Sw in the regenerator 132 evaporates and becomes concentrated solution Sa, and is stored in the 132c of storage portion.On the other hand, the cold-producing medium that evaporates from weak solution Sw is sent to condenser 33 as refrigerant vapour Vb.Be stored in the concentrated solution Sa of the 132c of storage portion,, be pressed and delivered to the concentrated solution spreading nozzle 131a of absorber 131 by solution pipe arrangement 155 by solution pump 138.In addition, for solution pump 138, its attached inverter 138x accepts liquid level signal from the weak solution liquid level detector 168 of absorber 131 at any time, when the liquid level of the weak solution Sw of the 131c of storage portion of absorber 131 is low, thereby makes rotary speed increase the ejection flow; When the liquid level of the weak solution Sw of the 131c of storage portion is high, thereby then make rotary speed reduce the ejection flow.The concentrated solution Sa that flows in solution pipe arrangement 155 rises temperature by carry out heat exchange with weak solution Sw in solution heat exchanger 136, afterwards, flow into absorber 131, and scatters from concentrated solution spreading nozzle 131a.Afterwards, repeat same circulation.
Below with reference to Fig. 5, the formation of the absorption heat pump 130A that the variation of the 4th embodiment of the present invention is related to describes.(a) is the system diagram of absorption heat pump 130A among Fig. 5, and (b) is the part details drawing of the introduction part flow separator 120 on every side of heated medium W among Fig. 5.Absorption heat pump 130A and absorption heat pump 130 (with reference to Fig. 4) are relatively, replacing mixing heated medium pipe 119A (with reference to Fig. 4) is connected with gas-liquid separator 120, and the mixing heated medium Wm that this mixing heated medium pipe 119A flows and has the part of heated medium liquid Wq in heated medium pipe 131a to become steam and obtain, heated medium supply pipe 119C is connected with gas-liquid separator 120, and this heated medium supply pipe 119C is as supplying with stream, being used for will be absorber 131 heated heated medium W guides to gas-liquid separator 120 as heated medium liquid Wq near, before importing gas-liquid separator 120, make the part gasification of heated medium liquid Wq and become and mix heated medium Wm.In heated medium supply pipe 119c, near gas-liquid separator 120, be provided with throttle orifice 119r as the decompressing unit of the part gasification that makes heated medium liquid Wq.Typically, the inlet 28 of gas-liquid separator 120 is inserted in the end of gas-liquid separator 120 sides of heated medium supply pipe 119c, is provided with throttle orifice 119r in the part that is inserted in the gas-liquid separator 120 of heated medium supply pipe 119C.The opening of end of heated medium supply pipe 119c that is inserted into the part in the gas-liquid separator 120 is relative with baffle plate 21.Insert at heated medium supply pipe 119C under the situation of inlet 28 of gas-liquid separator 120, the pipe end of heated medium supply pipe 119C and the border of inlet 28 become introducing port.In addition, the end of heated medium supply pipe 119C also can not inserted inlet 28 and is connected with the sidewall of main body 20B (in this case, also decompressing unit can be arranged to be positioned at sidewall identical faces) with main body 20B, in addition, also decompressing unit can be arranged to be positioned at the inside of heated medium supply pipe 119C of the outside of main body 20B.Decompressing unit can be arranged on the sidewall of main body 20B, also can be arranged near the heated medium supply pipe 119C of main body 20B.Decompressing unit also can be the structure (for example valve etc.) of the part decompression gasification that can make heated medium liquid Wq beyond the throttle orifice 119r.In addition, under the situation of the heated medium supply pipe 119C of the boundary member that decompressing unit is arranged at heated medium supply pipe 119C and gas-liquid separator 120, heated medium liquid Wq from heated medium supply pipe 119C when gas-liquid separator 120 flows into, the one partial gasification.But, establish this situation and also be contained in the situation that gas-liquid separator 120 imports mixing heated medium liquid Wm (fluid-mixing).The above-mentioned structure in addition of absorption heat pump 130A is identical with absorption heat pump 130 (with reference to Fig. 4).
In absorption heat pump 130A, become following temperature and pressure: the heated medium liquid Wq that is sent to absorber 131 by heated medium liquid pump 118, do not seethe with excitement even in heated medium pipe 131a, be heated yet, and flow into heated medium supply pipe 119c with the state of heated medium liquid Wq.For this reason, typically, ejection pressure to heated medium liquid pump 118 and/or additional heated medium pump 142 is set (or adjusting), so that the pressure in the heated medium pipe 131a becomes than the saturation pressure high pressure suitable with the temperature of heated medium liquid Wq.The heated medium liquid Wq that in heated medium supply pipe 119c, flows, before being imported into gas-liquid separator 120, by throttle orifice 119r, thus, pressure reduces, a part is seethed with excitement and is become heated medium steam Wv, as a whole, becomes heated medium liquid Wq and heated medium steam Wv and mixes later mixing heated medium Wm.The shape of throttle orifice 119r is determined as follows: the pressure of the inlet 28 of gas-liquid separator 120 is maintained at the pressure lower than saturation pressure, and this saturation pressure is suitable with the temperature of the heated medium liquid Wq that flows in heated medium supply pipe 119C.The mixing heated medium Wm that generates by throttle orifice 119r flows into the inlet 28 of gas-liquid separator 120, changes its flow direction with baffle plate 21 collisions that are present in the flow direction front.In addition, as decompressing unit, throttle orifice 119r is arranged under the situation of heated medium supply pipe 119C (the pipe end face of heated medium supply pipe 119C) of the boundary member of heated medium supply pipe 119C and gas-liquid separator 120, form under the situation of squit hole etc. of a plurality of heated medium liquid Wq with fore-end at heated medium supply pipe 119C, also sometimes, the state that heated medium liquid W presses heated medium liquid Wq flows into gas-liquid separator 120, the part of heated medium liquid Wq gasifies and becomes mixing heated medium Wm in gas-liquid separator 120, and this mixes heated medium Wm and baffle plate 21 collisions.After, identical with the situation of absorption heat pump 130 (with reference to Fig. 4), in gas-liquid separator 120, heated medium liquid Wq and heated medium steam Wv are separated, heated medium liquid Wq is imported into heated medium pipe 131a by recurrent canal 119B, and heated medium steam Wv is derived and be provided for the place that utilizes steam from export mouth 29e.The above-mentioned effect in addition of absorption heat pump 130A, (with reference to Fig. 4) is identical with absorption heat pump 130.
In the above description, if being the mode bending of " く " word shape (crest line is arranged), the side that bending plate 24 is seen to observe rectangular plate from short brink forms, yet also can be, to be N word shape (two crest lines are arranged), perhaps be that W (M) word shape (three crest lines are arranged) etc. has the mode of many crest lines to form from the observed side of short brink from the observed side of short brink.
Among Fig. 6 (a), being the horizontal cross of the main body 20B part of the gas-liquid separator that relates to of variation, is that two mode forms with the crest line of bending plate 24X.Among Fig. 6 (b), being the horizontal cross of the main body 20B part of the gas-liquid separator that relates to of another variation, is that three mode forms with the crest line of bending plate 24Y.The crest line of bending plate 24 (24X, 24Y) is many more, promptly between bending plate 24 (24X, 24Y) in the stream of formed crank-like, the change number of times of flow direction of refrigerant vapour Va of drop that contains concentrated solution Sa is many more, just can improve the effect of gas-liquid separation more.Yet, consider that from the viewpoint of the manufacturing cost that suppresses bending plate 24 (24X, 24Y) the bar number of crest line is better less.
In the above description, establishing plate-shaped member is the bending plate 24 (24X, 24Y) that a crest line is arranged, yet, also can be to form, the part on the mountain of bending plate 24 (24X, 24Y) does not connect the plate-shaped member 24Z that separates " Ha " word shape.
Among Fig. 6 (c), be the other horizontal cross of the main body 20B part of the gas-liquid separator that relates to of other variation, the top that sets the mountain that forms bending plate does not connect (discontinuous) and the plate-shaped member 24Z of " Ha " word shape of separating.In this case, inlet opening portion 23 and between plate-shaped member 24Z the refrigerant vapour Va of drop that flow in the formed stream, that contain concentrated solution Sa, temporarily the face from plate-shaped member 24Z leaves, but, with the face collision of the plate-shaped member 24Z that has changed direction (with respect to the angle of the face of dividing plate 22) and contact the back once more and change mobile direction, thereby the drop of concentrated solution Sa is separated.In addition, though omitted diagrammatic sketch, yet, as plate-shaped member, also can constitute: with porous plate (for example perforated board), with the stagger position in hole of the flow direction with respect to the refrigerant vapour Va of the drop that contains concentrated solution Sa, and its face and the rectangular mode that flows, devices spaced apart and disposing in the horizontal direction.
In the above description, if with bending plate 24, be installed on dividing plate 24 in the roughly vertical mode of its crest line, the refrigerant vapour Va of the drop that contains concentrated solution Sa that flows between bending plate 24 crawls in the horizontal direction, yet, also can be, bending plate 24 is installed on dividing plate 24 in the mode of its crest line approximate horizontal, the refrigerant vapour Va of the drop that contains concentrated solution Sa that flows between bending plate 24 crawls on vertical direction.In this case, lodge in the part of the paddy of bending plate 24 in order not make separated concentrated solution Sa, set as follows and get final product: observe bending plate 24 from the side and be " ヘ " word, promptly the top on the mountain of bending plate 24 is for the highest.
In the above description, baffled 21 constitute with dividing plate 22 one, yet, also can be baffle plate 21 is separated with dividing plate 22 and to constitute.
Fig. 7 is that expression separates baffle plate 21 and a main body 120B example partly of the gas-liquid separator that constitutes with dividing plate 22.Main body 120B compares with main body 20B (referring to (a) among Fig. 1), and it is shorter to form vertical direction, and horizontal direction is longer.With baffle plate 21 set into; separate with dividing plate 22, stop from the position of flowing of fluid-mixing introducing port 28d to the fluid-mixing Fm of peristome 23 in order to make fluid-mixing Fm and its collision, to be provided in; in order to ensure the stream of fluid-mixing Fm, and leave from sidewall and the top board of main body 120B.The gas-liquid separator that possesses the main body 120B of this variation, compare with the gas-liquid separator 20 that possesses main body 20B (referring to (a) among Fig. 1), big in the horizontal direction, yet, owing to can suppress height dimension, and possess the dividing plate 22 that comprises plate-shaped member 24, therefore compare, become separator small-sized and the gas-liquid separation superior performance with gas-liquid separator in the past.
In the above description, establishing high-temp regenerator 32A is tubular regenerator, yet also can be Natural Circulation liquid tubular type regenerator or forced circulation liquid tubular type regenerator, perhaps fume tube type regenerator.Even the regenerator except that tubular regenerator by possessing gas-liquid separator 20, also can improve the separating effect of refrigerant vapour Va and concentrated solution Sa.In addition, also can be with the gas-liquid separator that the present invention relates to, when being used for compression refrigerating machine, be used for gas-liquid mixed refrigerant is separated into as the refrigerant gas of gas with as the purposes of the refrigerant liquid of liquid.It is constructed as follows.That is, this gas-liquid separator is behind compression refrigerant gas compression refrigerating machine and in the gas-liquid mixed refrigerant that produces, refrigerant gas is separated with refrigerant liquid; This gas-liquid separator possesses: baffle plate, and it makes the above-mentioned gas-liquid mixed refrigerant that imported with its collision and separate above-mentioned refrigerant liquid; Dividing plate, it will be divided into inlet and downstream chamber in the gas-liquid separator, this inlet has formed the introducing port that is used to import above-mentioned gas-liquid mixed refrigerant, this downstream chamber has formed the refrigerant gas export mouth that is used for deriving the above-mentioned refrigerant gas that separates from above-mentioned mix refrigerant, this dividing plate comprises plate-shaped member and constitutes, and this plate-shaped member is used to make above-mentioned gas-liquid mixed refrigerant and its collision that utilizes above-mentioned baffle plate and separated above-mentioned refrigerant liquid, further separates above-mentioned refrigerant liquid.As embodiment, it constitutes, and in Fig. 1, flows into gas-liquid mixed refrigerant from fluid-mixing introducing port 28d, from refrigerant vapour export mouth 29e refrigerant gas is flowed out, and takes out refrigerant liquid from solution export mouth 20n.Also can not establish reflux solution export mouth 20r.In addition, the gas-liquid separator that the present invention relates to also goes for steam boiler, particularly through-flow boiler.
In the above description, Absorption Refrigerator 30 is made as double-effect absorption refrigerating machine is illustrated, yet also can be single-effective absorption refrigerating machine or three-effect absorption-type refrigeration machine.Under the situation of single-effective absorption refrigerating machine, can be with the high-temp regenerator 32A that illustrates in the present embodiment as regenerator, under the situation of three-effect absorption-type refrigeration machine, also can be with the high-temp regenerator 32A that illustrates in the present embodiment, as the highest regenerator of actuation temperature.
In the above description, the absorption heat pump that absorption heat pump 130 is made as single-stage is illustrated, yet also can be multistage absorption heat pump.In addition, if supply to the additional heated medium Ws of gas-liquid separator 120, preheating in heat exchanger 143,144, yet, also can be before heat exchanger 143,144 or alternative heat exchanger 143,144, by condenser 133 and/or evaporimeter 134, utilize the heat of refrigerant vapour Vb and/or refrigerant vapour Ve to carry out preheating.
Claims (9)
1. gas-liquid separator separates above-mentioned gas and aforesaid liquid from mixed the fluid-mixing that gas obtains with liquid, it is characterized in that possessing:
Baffle plate is used to make the above-mentioned fluid-mixing that imported with its collision and separate aforesaid liquid;
Dividing plate, it will be divided into inlet and downstream chamber in the above-mentioned gas-liquid separator, wherein inlet is formed with the introducing port that is used to import above-mentioned fluid-mixing, the downstream chamber is formed with the gas export mouth that is used for deriving the above-mentioned gas that separates from above-mentioned fluid-mixing, this dividing plate comprises plate-shaped member and constitutes, and this plate-shaped member is used to make above-mentioned fluid-mixing and its collision that utilizes above-mentioned baffle plate and separated aforesaid liquid, further separates aforesaid liquid.
2. gas-liquid separator according to claim 1 is characterized in that,
Above-mentioned baffle plate and aforementioned barriers one constitute;
Bottom in above-mentioned inlet and above-mentioned downstream chamber is formed with the connected entrance that is communicated with above-mentioned inlet and above-mentioned downstream chamber;
Below the lower end of above-mentioned introducing port and be formed at the above-mentioned downstream chamber side of the peristome of aforementioned barriers, arrange along the face of aforementioned barriers and be equipped with a plurality of above-mentioned plate-shaped members.
3. gas-liquid separator according to claim 2 is characterized in that,
Above-mentioned plate-shaped member is to set in the roughly vertical mode of crest line that forms by bending.
4. according to any described gas-liquid separator in the claim 1 to 3, it is characterized in that,
Possesses liquid level detector, be stored in the liquid level of the liquid in the above-mentioned gas-liquid separator and send signal in order to detection, to keep above-mentioned connected entrance to submerge being stored in the state in the liquid in the above-mentioned gas-liquid separator to the control device of the liquid level that is used to control the liquid in the above-mentioned gas-liquid separator.
5. a high-temp regenerator is characterized in that,
Above-mentioned gas is the refrigerant vapour that produces by heat dilute solution;
Aforesaid liquid is to produce the concentrated solution that above-mentioned refrigerant vapour makes concentration rise and obtain by heating above-mentioned weak solution;
This high-temp regenerator also possesses: any described gas-liquid separator in the claim 1 to 4;
With the liquid chamber that holds above-mentioned weak solution,
Be formed with the phegma export mouth in the bottom of above-mentioned gas-liquid separator, be used for separated above-mentioned concentrated solution is derived to above-mentioned liquid chamber.
6. Absorption Refrigerator is characterized in that possessing:
The described high-temp regenerator of claim 5;
Condenser is used to the refrigerant vapour that condenses;
Evaporimeter, it imports the refrigerant liquid that condenses in above-mentioned condenser, and utilizes the heat of the medium that is cooled to make above-mentioned refrigerant liquid evaporation;
Absorber, it imports above-mentioned concentrated solution, and is absorbed in the cold-producing medium that evaporates in the above-mentioned evaporimeter and above-mentioned strong solution concentration is reduced and the weak solution that obtains derives to above-mentioned liquid chamber with above-mentioned concentrated solution.
7. absorption heat pump is characterized in that possessing:
Absorber, it has makes heated medium flow to inner heated medium stream, absorption liquid absorption refrigeration agent steam, and heat the above-mentioned heated medium that in above-mentioned heated medium stream, flows, make above-mentioned heated medium become gas from liquid;
Gas-liquid separator, it is any described gas-liquid separator in the claim 1 to 4, it imports fluid, and above-mentioned gas is the above-mentioned heated medium of gas, aforesaid liquid is the above-mentioned heated medium of liquid, above-mentioned fluid is that this gas-liquid separator separates the heated medium of above-mentioned gas and the heated medium of aforesaid liquid from the heated medium of the above-mentioned gas of above-mentioned heated medium stream derivation and the mixed fluid of heated medium of aforesaid liquid;
The backflow stream, the heated medium of the aforesaid liquid that it will separate in above-mentioned gas-liquid separator guides to above-mentioned heated medium stream.
8. absorption heat pump is characterized in that possessing:
Absorber, it has makes heated medium flow to inner heated medium stream, absorption liquid absorption refrigeration agent steam, and heat the above-mentioned heated medium that in above-mentioned heated medium stream, flows;
Decompressing unit, it makes the above-mentioned heated medium decompression by above-mentioned absorber heating, and makes the one partial gasification;
Gas-liquid separator, it is any described gas-liquid separator in the claim 1 to 4, it imports fluid, and above-mentioned gas is the above-mentioned heated medium of gas, aforesaid liquid is the above-mentioned heated medium of liquid, above-mentioned fluid is that this gas-liquid separator separates the heated medium of above-mentioned gas and the heated medium of aforesaid liquid by the heated medium of the above-mentioned gas of above-mentioned decompressing unit generation and the mixed fluid of heated medium of aforesaid liquid;
The backflow stream, the heated medium of the aforesaid liquid that it will separate in above-mentioned gas-liquid separator guides to above-mentioned heated medium stream.
9. absorption heat pump is characterized in that possessing:
Absorber, it has makes heated medium flow to inner heated medium stream, absorption liquid absorption refrigeration agent steam, and heat the above-mentioned heated medium that in above-mentioned heated medium stream, flows;
Gas-liquid separator, it is any described gas-liquid separator in the claim 1 to 4, it constitutes, replacement imports above-mentioned fluid-mixing from above-mentioned introducing port, importing is by the heated medium of the aforesaid liquid of above-mentioned absorber heating, and above-mentioned gas is the above-mentioned heated medium of gas, and aforesaid liquid is the above-mentioned heated medium of liquid;
The backflow stream, the heated medium of the aforesaid liquid that it will separate in above-mentioned gas-liquid separator guides to above-mentioned heated medium stream,
Above-mentioned gas-liquid separator constitutes, make the aforesaid liquid that has imported heated medium part gasification and become above-mentioned fluid-mixing, from above-mentioned fluid-mixing, separate the heated medium of above-mentioned gas and the heated medium of aforesaid liquid.
Applications Claiming Priority (6)
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| JP2007215367 | 2007-08-22 | ||
| JP2007215367 | 2007-08-22 | ||
| JP2007-215367 | 2007-08-22 | ||
| JP2008185676 | 2008-07-17 | ||
| JP2008-185676 | 2008-07-17 | ||
| JP2008185676 | 2008-07-17 |
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| CN101373115A true CN101373115A (en) | 2009-02-25 |
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| CN2008102140010A Active CN101373115B (en) | 2007-08-22 | 2008-08-22 | Gas-liquid separator, high temperature regenerator, absorption type refrigerator and absorption type heatpump |
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| CN (1) | CN101373115B (en) |
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| CN107228502A (en) * | 2016-03-23 | 2017-10-03 | 荏原冷热系统株式会社 | Absorption heat pump |
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Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS61262566A (en) * | 1985-05-16 | 1986-11-20 | ダイキン工業株式会社 | Absorption type refrigerator |
| JP3824373B2 (en) * | 1997-04-09 | 2006-09-20 | 大阪瓦斯株式会社 | Regeneration part structure in ammonia absorption refrigerator. |
| JP2004176968A (en) * | 2002-11-26 | 2004-06-24 | Kubota Corp | Vapor-liquid separator |
| JP4519744B2 (en) * | 2005-09-21 | 2010-08-04 | 荏原冷熱システム株式会社 | High temperature regenerator and absorption refrigerator |
-
2008
- 2008-08-21 JP JP2008212465A patent/JP5261073B2/en active Active
- 2008-08-22 CN CN2008102140010A patent/CN101373115B/en active Active
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| CN107228502A (en) * | 2016-03-23 | 2017-10-03 | 荏原冷热系统株式会社 | Absorption heat pump |
| CN107228502B (en) * | 2016-03-23 | 2020-10-23 | 荏原冷热系统株式会社 | Absorption heat pump |
| CN107270585A (en) * | 2016-04-06 | 2017-10-20 | 荏原冷热系统株式会社 | Absorption heat pump |
| CN110337326A (en) * | 2017-04-13 | 2019-10-15 | 株式会社堀场Stec | Gasification installation and gasification system |
| CN107166825A (en) * | 2017-06-30 | 2017-09-15 | 美的集团武汉制冷设备有限公司 | Flash vessel and air-conditioning system |
| CN111156731A (en) * | 2020-01-03 | 2020-05-15 | 北京市伟业供热设备有限责任公司 | Absorption type cold and hot water unit |
| CN112263850A (en) * | 2020-09-30 | 2021-01-26 | 青岛双瑞海洋环境工程股份有限公司 | Gas-liquid separation device for sodium hypochlorite generator |
| CN112263850B (en) * | 2020-09-30 | 2022-04-26 | 青岛双瑞海洋环境工程股份有限公司 | Gas-liquid separation device for sodium hypochlorite generator |
| CN113686052A (en) * | 2021-08-16 | 2021-11-23 | 山东大学 | Intelligent control open type compression absorption heat pump system for water and waste heat recovery |
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Also Published As
| Publication number | Publication date |
|---|---|
| CN101373115B (en) | 2012-11-21 |
| JP5261073B2 (en) | 2013-08-14 |
| JP2010043819A (en) | 2010-02-25 |
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