JPH02298767A - Absorption refrigerator - Google Patents
Absorption refrigeratorInfo
- Publication number
- JPH02298767A JPH02298767A JP12010489A JP12010489A JPH02298767A JP H02298767 A JPH02298767 A JP H02298767A JP 12010489 A JP12010489 A JP 12010489A JP 12010489 A JP12010489 A JP 12010489A JP H02298767 A JPH02298767 A JP H02298767A
- Authority
- JP
- Japan
- Prior art keywords
- concentrating
- absorption liquid
- absorption
- absorbent
- absorber
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 60
- 239000007788 liquid Substances 0.000 claims abstract description 39
- 230000002745 absorbent Effects 0.000 claims abstract description 21
- 239000002250 absorbent Substances 0.000 claims abstract description 21
- -1 compound salts Chemical class 0.000 claims abstract description 14
- 229910052736 halogen Inorganic materials 0.000 claims abstract description 8
- 150000002367 halogens Chemical class 0.000 claims abstract description 8
- 229910052731 fluorine Inorganic materials 0.000 claims abstract description 6
- 229910052744 lithium Inorganic materials 0.000 claims abstract description 6
- 229910052794 bromium Inorganic materials 0.000 claims abstract 4
- 229910052801 chlorine Inorganic materials 0.000 claims abstract 4
- 229910052700 potassium Inorganic materials 0.000 claims abstract 3
- 238000005057 refrigeration Methods 0.000 claims description 18
- 239000006096 absorbing agent Substances 0.000 claims description 16
- 239000012528 membrane Substances 0.000 claims description 14
- 238000001223 reverse osmosis Methods 0.000 claims description 7
- 239000004952 Polyamide Substances 0.000 claims description 5
- 239000004721 Polyphenylene oxide Substances 0.000 claims description 5
- 229910052783 alkali metal Inorganic materials 0.000 claims description 5
- 150000001340 alkali metals Chemical class 0.000 claims description 5
- 229910052784 alkaline earth metal Inorganic materials 0.000 claims description 5
- 150000001342 alkaline earth metals Chemical class 0.000 claims description 5
- 229910052791 calcium Inorganic materials 0.000 claims description 5
- 229920002678 cellulose Polymers 0.000 claims description 5
- 239000001913 cellulose Substances 0.000 claims description 5
- 229910052749 magnesium Inorganic materials 0.000 claims description 5
- 150000002894 organic compounds Chemical class 0.000 claims description 5
- 229920002647 polyamide Polymers 0.000 claims description 5
- 229920002614 Polyether block amide Polymers 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 7
- 230000007935 neutral effect Effects 0.000 abstract description 4
- 239000002253 acid Substances 0.000 abstract description 3
- 239000000446 fuel Substances 0.000 abstract description 3
- 238000012423 maintenance Methods 0.000 abstract description 3
- 239000002184 metal Substances 0.000 abstract 2
- 229910052751 metal Inorganic materials 0.000 abstract 2
- 230000003628 erosive effect Effects 0.000 abstract 1
- 238000007654 immersion Methods 0.000 abstract 1
- 238000007689 inspection Methods 0.000 abstract 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 24
- 239000000110 cooling liquid Substances 0.000 description 11
- 239000002826 coolant Substances 0.000 description 8
- 239000000498 cooling water Substances 0.000 description 5
- 239000011575 calcium Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 2
- 229910001622 calcium bromide Inorganic materials 0.000 description 2
- WGEFECGEFUFIQW-UHFFFAOYSA-L calcium dibromide Chemical compound [Ca+2].[Br-].[Br-] WGEFECGEFUFIQW-UHFFFAOYSA-L 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 231100001261 hazardous Toxicity 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 description 2
- KWGKDLIKAYFUFQ-UHFFFAOYSA-M lithium chloride Chemical compound [Li+].[Cl-] KWGKDLIKAYFUFQ-UHFFFAOYSA-M 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229920000570 polyether Polymers 0.000 description 2
- 230000002265 prevention Effects 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- 229920000742 Cotton Polymers 0.000 description 1
- MBHNWCYEGXQEIT-UHFFFAOYSA-N Fluphenazine hydrochloride Chemical compound Cl.Cl.C1CN(CCO)CCN1CCCN1C2=CC(C(F)(F)F)=CC=C2SC2=CC=CC=C21 MBHNWCYEGXQEIT-UHFFFAOYSA-N 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 238000004378 air conditioning Methods 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000008602 contraction Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
Landscapes
- Sorption Type Refrigeration Machines (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、蒸発器、吸収器、濃縮部を管路により後続し
て冷凍サイクルを構成し、濃縮部における稀釈吸収液の
濃縮手段を逆浸透法による濃縮手段にした吸収冷凍装置
に関する。[Detailed Description of the Invention] [Industrial Application Field] The present invention comprises a refrigeration cycle in which an evaporator, an absorber, and a concentrating section are connected through a pipe, and the means for concentrating the diluted absorption liquid in the concentrating section is reversed. This invention relates to an absorption refrigeration device using a osmosis method as a concentration means.
従来の吸収冷凍装置は、第２図に示すように構成されて
いる。A conventional absorption refrigeration system is constructed as shown in FIG.
系全体は真空状態でおり、蒸発器（１）において。The whole system is under vacuum, in the evaporator (1).
純水からなる冷却液（２）を冷却液散水ポンプ（３）、
冷却液循環パイプ（４）、流量調整弁（５）を経て冷却
液散水器（６）から蒸発器（１）内に散水する。Cooling liquid (2) consisting of pure water is passed through a cooling liquid sprinkler pump (3),
Water is sprinkled into the evaporator (1) from a coolant sprinkler (6) via a coolant circulation pipe (4) and a flow rate adjustment valve (5).
このとき、蒸発器（１）内が真空状態のため、水滴は蒸
発器（１）内、の伝熱管（７）内の水から気化熱を奪い
ながら蒸発し、伝熱管（７）内の水が冷却し、冷房用の
冷水として使用される。At this time, since the inside of the evaporator (1) is in a vacuum state, the water droplets evaporate while taking vaporization heat from the water inside the heat exchanger tube (7) inside the evaporator (1). is used as cold water for air conditioning.
一方、冷却液（２）の蒸発した水蒸気は１通路（８）を
通って吸収器（９）に導入する。On the other hand, the evaporated water vapor of the cooling liquid (2) is introduced into the absorber (9) through one passage (8).
吸収器（９）において、濃縮された吸収液ａＯが吸収液
散水器Ｑυから散水され、水蒸気が吸収液Ｏｑに吸収さ
れる。In the absorber (9), the concentrated absorption liquid aO is sprinkled from an absorption liquid sprinkler Qυ, and water vapor is absorbed into the absorption liquid Oq.
このとき、吸収液００は作動温度によって吸収剤の種類
や濃度が異なり、臭化リチウム、塩化リチウム等の水溶
液又は臭化カルシウム、塩化カルシウム等の濃水溶液が
用いられ２臭化リチウムの場合３０〜７０％の範囲、臭
化カルシウムの場合４０〜７０％の範囲で使用される。At this time, the type and concentration of the absorbent in the absorption liquid 00 differs depending on the operating temperature, and an aqueous solution of lithium bromide, lithium chloride, etc. or a concentrated aqueous solution of calcium bromide, calcium chloride, etc. is used. It is used in the range of 70%, and in the case of calcium bromide in the range of 40-70%.
また、吸収器（９ｉ内は水蒸気と吸収液００との接触面
積を大にするため、吸収液ＱＱの７ヤワリングや延面滴
下等を行い、水蒸気の吸収を容易にする。In addition, in order to increase the contact area between the water vapor and the absorption liquid 00 in the absorber (9i), the absorption liquid QQ is subjected to 7 Yawaring or dripping on the entire surface to facilitate the absorption of water vapor.
そして、吸収器（９）Ｋおける水蒸気の吸収により真空
状態が維持され、蒸発器（１）における冷却液（２）の
蒸発及び吸収器（９）における水蒸気の吸収が継続され
る。The vacuum state is maintained by the absorption of water vapor in the absorber (9)K, and the evaporation of the cooling liquid (2) in the evaporator (1) and the absorption of water vapor in the absorber (9) continue.
さらに、吸収器（９）内の伝熱管（２）に止弁ａ］から
冷却水が流通し２吸収液α０の吸収熱が伝熱管（２）内
の冷却水に吸収される。Further, cooling water flows through the heat transfer tube (2) in the absorber (9) from the stop valve a], and the absorbed heat of the second absorption liquid α0 is absorbed by the cooling water in the heat transfer tube (2).
一方、水蒸気を吸収し濃度の低下した稀釈吸収液（１４
）は、吸収液循環ボンデ０５．吸収液循環パイプＱｅ、
止弁ａη及び熱交換器（至）を経て濃縮器四に流入する
。On the other hand, the diluted absorption liquid (14
) is an absorbent circulation bonder 05. Absorbent circulation pipe Qe,
It flows into the concentrator 4 via the stop valve aη and the heat exchanger (to).
この濃縮器０１において、稀釈吸収液α→は加熱用バー
ナ（７）により加熱され、吸収した水蒸気を放出し、濃
縮された吸収液ＱＯとなり、熱交換器（ト）、吸収液循
環パイプ＠、吸収液散水ポンプ翰、流量調整弁−を経て
散水器θυから濃縮吸収液αりが散水される。In this concentrator 01, the diluted absorption liquid α→ is heated by a heating burner (7), releases the absorbed water vapor, and becomes a concentrated absorption liquid QO, which is transferred to a heat exchanger (g), an absorption liquid circulation pipe @, The concentrated absorption liquid α is sprinkled from the water sprinkler θυ via the absorption liquid sprinkler pump and the flow rate adjustment valve.
そして、濃縮器（１すにおいて放出された水蒸気は。The water vapor released in the condenser (1) is
通路（ハ）を通って膨縮″ａ（ホ）に流入する。It flows through the passage (c) into the expansion/contraction "a" (e).
一方、吸収器（９）の伝熱管＠は冷却水循環バイブ（ホ
）を介して凝縮器曽内の伝熱管翰に接続されており、伝
熱管■内の冷却水により水蒸気が冷却されて冷却液（２
）となシ、冷却液循環パイプ弼、冷却液循環ボンデ翰、
止弁（至）を経て蒸発器（１）に流入する。On the other hand, the heat exchanger tubes @ of the absorber (9) are connected to the heat exchanger tubes in the condenser via the cooling water circulation vibrator (E), and the water vapor is cooled by the cooling water in the heat exchanger tubes and the cooling liquid is (2
)tonashi, coolant circulation pipe 2, coolant circulation bonder,
It flows into the evaporator (1) through the stop valve (to).
以上、蒸発器（１）、吸収器（９）、濃縮器０Ｉ及び凝
縮器（ハ）が管路により接続されて冷凍サイクルが構成
されている。As described above, the evaporator (1), the absorber (9), the concentrator 0I, and the condenser (c) are connected by a pipe to constitute a refrigeration cycle.
ところで、従来の装置は、稀釈吸収液ａ４の濃縮に、濃
縮器０呻において加熱用バーナーによる蒸発法を用いて
いるため、成績係数が悪く、かつ、火力によるため適用
上の制約があり、さらに、排ガスの処理、燃料洩れ対策
、火災防止、保守管理等。By the way, the conventional apparatus uses an evaporation method using a heating burner in the concentrator 0 to concentrate the diluted absorption liquid A4, so the coefficient of performance is poor, and there are restrictions on application because it relies on thermal power. , exhaust gas treatment, fuel leakage prevention, fire prevention, maintenance management, etc.
種々の問題点がある。There are various problems.
そこで１本発明者等は特願昭６８−８０５４５０の吸収
冷凍装置において、濃縮部における稀釈吸収液の濃縮手
段を逆浸透法による濃縮手段にすることを発明した。Therefore, the inventors of the present invention invented a method of concentrating the diluted absorption liquid in the concentrating section in an absorption refrigerating apparatus disclosed in Japanese Patent Application No. 68-805450 using a reverse osmosis method.
その１例は、第１図に示す通りであシ、第２図の場合と
同様、系全体は真空状態であり、同様の冷却液（２）、
吸収液ＱＯが使用され、貯留槽０υの冷却液（２）が冷
却液循環パイプ暁、冷却液散水ボンデ（３）。An example of this is as shown in Figure 1. As in Figure 2, the entire system is in a vacuum state, and the same coolant (2),
The absorption liquid QO is used, and the cooling liquid (2) in the storage tank 0υ is connected to the cooling liquid circulation pipe (Xiao), and the cooling liquid watering bond (3).
流量調整弁（５）を経て蒸発器（１）内の冷却液散水器
（６）から散水され、水滴が伝熱管（７）内の水から気
化熱を奪って蒸発する。Water is sprayed from the cooling liquid sprinkler (6) in the evaporator (1) via the flow rate adjustment valve (5), and the water droplets take the heat of vaporization from the water in the heat transfer tube (7) and evaporate.
冷却液（２）の蒸発した水蒸気は通路（８）を通って吸
収器（９）に導入し、濃縮吸収液Ｏｑが吸収液循環バイ
ブぐυ、吸収液散水ポンプ翰、流量調整弁（ホ）を経て
吸収液散水器０ηから吸収器（９）内に散水し、水蒸気
が吸収液ＱＱに吸収され、伝熱管口内の冷却水により吸
収液ｑＱの吸収熱が吸収される。The evaporated water vapor of the cooling liquid (2) is introduced into the absorber (9) through the passage (8), and the concentrated absorption liquid Oq is passed through the absorption liquid circulation vibrator Gυ, the absorption liquid sprinkler pump head, and the flow rate adjustment valve (H). Water is sprinkled into the absorber (9) from the absorption liquid sprinkler 0η, the water vapor is absorbed by the absorption liquid QQ, and the heat of absorption of the absorption liquid qQ is absorbed by the cooling water in the mouth of the heat transfer tube.
水蒸気を吸収した稀釈吸収液ａΦは、吸収液循環ポンプ
叫、吸収液循環パイプＯｅ、止弁αη及び熱交換器（ト
）を経て濃縮部（３３１に流入する。The diluted absorption liquid aΦ that has absorbed water vapor flows into the concentration section (331) through the absorption liquid circulation pump, the absorption liquid circulation pipe Oe, the stop valve αη, and the heat exchanger (g).
この濃縮部ωにおいて、半透膜□□□による逆浸透法か
らなる濃一手段により、稀釈吸収液Ｃ１４１中の水が半
透膜岨）を透過して移動し、稀釈吸収液Ｑ４１が濃縮さ
れた吸収液０Ｑとなり、吸収液循環パイプμｓを経て熱
交換器（至）に流入する。In this concentration section ω, the water in the diluted absorption liquid C141 passes through the semipermeable membrane □□□ and moves through the semipermeable membrane □□□, and the diluted absorption liquid Q41 is concentrated. The absorbent liquid 0Q flows into the heat exchanger through the absorbent circulation pipe μs.
そして、濃縮部酷において半透膜（資）を透過した水、
すなわち冷却液（２）は貯留槽０］）に流入する。Then, the water that has passed through the semipermeable membrane (material) in the concentration section,
That is, the cooling liquid (2) flows into the storage tank 0]).
一方、蒸発器（１）の底部の冷却液（２）は、冷却液循
環パイプ（１）、冷却液循環ボンデσ、止弁駕及び逆止
弁翰を経て吸収液循環パイプｑＱの稀釈吸収液θ尋に合
流する。On the other hand, the coolant (2) at the bottom of the evaporator (1) passes through the coolant circulation pipe (1), the coolant circulation bond σ, the stop valve cage, and the check valve holder, and is then transferred to the diluted absorption liquid in the absorption liquid circulation pipe qQ. Join θ fathom.
すなわち、稀釈吸収液０弔の製綿ｊ手段が、濃縮部Ｃ３
３１における逆浸透法による濃縮手段であるため。That is, the cotton making means with 0 diluted absorbent is used in the concentration section C3.
Because it is a concentration method using reverse osmosis method in 31.
成績係数が第２図に比しきわめて高く、かつ、火力を用
いないため適用上の制約を受けず、さらに。The coefficient of performance is extremely high compared to Figure 2, and since no firepower is used, there are no restrictions on application.
第２図のような排ガス、燃料洩れ、火災等を考慮する必
要がなく、保守管理を容易にすることができる。There is no need to consider exhaust gas, fuel leakage, fire, etc. as shown in FIG. 2, and maintenance management can be facilitated.
第１図の逆浸透法による場合、使用する吸収剤及び半透
膜に種々の制約がある。When using the reverse osmosis method shown in FIG. 1, there are various restrictions on the absorbent and semipermeable membrane used.
すなわち吸収剤として２強酸１強アルカリ性物質の中に
優れた吸収特性を有するものが多数あるが、それ等の物
質では半透膜が堪えることができなく２他の部品の耐食
性にも問題があり、かつ。In other words, there are many absorbents that have excellent absorption properties, such as 2 strong acids, 1 strong alkalinity, but these materials cannot withstand semipermeable membranes, and 2 have problems with the corrosion resistance of other parts. ,and.
取扱い上も有害、危険なものも多い。Many of them are harmful and dangerous to handle.
また、半透膜として、吸収剤の濃縮に不適当で不安定な
もの、比較的製作が困難であり、入手が容易でないもの
がある。Additionally, some semipermeable membranes are unsuitable and unstable for concentrating absorbents, others are relatively difficult to manufacture, and some are not easily available.
本発明は、前記の点に留意してなされたものである。The present invention has been made with the above points in mind.
前記課題を解決するために２本発明の吸収冷凍装置は、
蒸発器、吸収器、濃縮部を管路により接続して冷凍サイ
クルを構成し、前記濃縮部における稀釈吸収液の濃縮手
段を逆浸透法による濃縮手段にした吸収冷凍装置におい
て。In order to solve the above problems, the absorption refrigeration apparatus of the present invention has the following features:
An absorption refrigeration apparatus in which an evaporator, an absorber, and a concentrator are connected through a pipe line to constitute a refrigeration cycle, and the means for concentrating the diluted absorption liquid in the concentrator is a concentrating means by reverse osmosis.
前記濃縮手段の吸収剤を、Ｌｉ、に等のアルカリ金属と
Ｆ、Ｃ１，Ｂｒ等ハロゲンの化合塩類としたものである
。The absorbent of the concentration means is a compound salt of an alkali metal such as Li and halogen such as F, C1, and Br.
また、前記濃縮手段の吸収剤を、Ｍｇ、Ｃａ等のアルカ
リ土金属、！： Ｆ 、 Ｃ１、Ｂｒ等ハロゲンの化合
塩類としたものである。Further, the absorbent of the concentration means may be an alkaline earth metal such as Mg or Ca! : Compound salts of halogens such as F, C1, Br, etc.
さらに、前記＃樹手段の半透膜を、セルロース系、ポリ
エーテル系、ポリアミド系等の有機化合物系にしたもの
である。Furthermore, the semi-permeable membrane of the above-mentioned resin means is made of an organic compound such as cellulose, polyether, or polyamide.
前記のように構成された本発明の吸収冷凍装置は、吸収
剤がＬｉ、に等のアルカリ金属又はＭｇ 、 Ｃａ等の
アルカリ土金属とＦ 、 ＣＩ 、 Ｂｒ等ハロゲンの
化合塩類からなるため１強酸２強アルカリ性でなくほぼ
中性であり、半透膜及び他の部品を侵食することなく、
取扱いが容易で危険がなく、吸収特性も良好である。The absorption refrigeration system of the present invention configured as described above is characterized by the fact that the absorbent is composed of compound salts of alkali metals such as Li and Ni or alkaline earth metals such as Mg and Ca, and halogens such as F, CI, and Br. 2. It is not strongly alkaline but almost neutral, and does not corrode semipermeable membranes and other parts.
It is easy to handle, non-hazardous, and has good absorption properties.
また、半透膜がセルロース系、ポリエーテル系。In addition, the semipermeable membrane is cellulose-based or polyether-based.
ポリアミド系等の有機化合物系であるため、吸収剤のｆ
ｉｋｌに最適で安定性を有し、！ｌ！ｌｉｉ作及び入手
が容易で経済性に優れている。Because it is based on organic compounds such as polyamide, the absorbent f
Ideal for ikl and has stability! l! It is easy to make and obtain, and is highly economical.
（実施例１）
濃縮手段の吸収剤を、Ｌｉ、に等のアルカリ金属とＦ
、 Ｃ９、Ｂｒ等ハロゲンの化合塩類とした。(Example 1) The absorbent of the concentration means is made of alkali metals such as Li and F.
, C9, Br, and other halogen compound salts.
（実施例２） 吸収剤を、Ｍｇ、Ｃａ等のアルカリ土金属とＦ。(Example 2) The absorbent is made of alkaline earth metals such as Mg and Ca and F.
Ｃ１、Ｂｒ等ハロゲンの化合塩類とした。Compound salts of halogens such as C1 and Br were used.
（実施例３）
半透膜を、セルロース系、ポリエーテル系、ポリアミド
系等の有機化合物系にした。(Example 3) The semipermeable membrane was made of an organic compound such as cellulose, polyether, or polyamide.
本発明は１以上説明したように構成されているので、以
下に記載する効果を奏する。Since the present invention is constructed as described in one or more of the above descriptions, it achieves the advantages described below.
吸収剤がＬｉ、に等のアルカリ金属又はＭｇ 、 Ｃａ
等のアルカリ土金属とＦ 、 Ｃ６、Ｂｒ等ハロゲンの
化合塩類からなるため１強酸１強アルカリ性でなくほぼ
中性であり、半透膜及び他の部品を侵食することなく、
取扱いが容易で危険がなく、吸収特性も良好である。Absorbent is alkali metal such as Li, Mg, Ca
It is composed of compound salts of alkaline earth metals such as F, C6, Br, etc., so it is not a strong acid or a strong alkaline, but is almost neutral, and does not corrode semipermeable membranes and other parts.
It is easy to handle, non-hazardous, and has good absorption properties.
また、半透膜がセルロース系、ポリエーテル系。In addition, the semipermeable membrane is cellulose-based or polyether-based.
ポリアミド系等の有機化合物系であるため、吸収剤の１
１組に最適で安定性を有し、製作及び入手が容易で経済
性に優れている。Since it is based on organic compounds such as polyamide, the absorbent
It is suitable for one set, has stability, is easy to manufacture and obtain, and is economical.
第１図゛は本発明が適用される吸収冷凍装置の１例の系
統図、第２図は従来例の系統図である。
（１）・・・蒸発器、（９）・・・吸収器、００・・・
吸収液、■・・・濃縮部、□□□・・・半透膜。FIG. 1 is a system diagram of an example of an absorption refrigeration system to which the present invention is applied, and FIG. 2 is a system diagram of a conventional example. (1)...Evaporator, (9)...Absorber, 00...
Absorption liquid, ■...concentration section, □□□...semipermeable membrane.
Claims (3)
凍サイクルを構成し、前記濃縮部における稀釈吸収液の
濃縮手段を逆浸透法による濃縮手段にした吸収冷凍装置
において、 前記濃縮手段の吸収剤を、Ｌｉ、Ｋ等のアルカリ金属と
Ｆ、Ｃｌ、Ｂｒ等ハロゲンの化合塩類とした吸収冷凍装
置。(1) An absorption refrigeration apparatus in which an evaporator, an absorber, and a concentrating section are connected by a pipe to form a refrigeration cycle, and the means for concentrating the diluted absorption liquid in the concentrating section is a means for concentrating the diluted absorption liquid by reverse osmosis. An absorption refrigeration device in which the absorbent is a compound salt of an alkali metal such as Li or K and a halogen such as F, Cl or Br.
凍サイクルを構成し、前記濃縮部における稀釈吸収液の
濃縮手段を逆浸透法による濃縮手段にした吸収冷凍装置
において、 前記濃縮手段の吸収剤を、Ｍｇ、Ｃａ等のアルカリ土金
属とＦ、Ｃｌ、Ｂｒ等ハロゲンの化合塩類とした吸収冷
凍装置。(2) An absorption refrigeration apparatus in which an evaporator, an absorber, and a concentrating section are connected by a pipe to constitute a refrigeration cycle, and the means for concentrating the diluted absorption liquid in the concentrating section is a means for concentrating the diluted absorption liquid by reverse osmosis. An absorption refrigeration device in which the absorbent is a compound salt of alkaline earth metals such as Mg and Ca and halogens such as F, Cl and Br.
凍サイクルを構成し、前記濃縮部における稀釈吸収液の
濃縮手段を逆浸透法による濃縮手段にした吸収冷凍装置
において、 前記濃縮手段の半透膜を、セルロース系、ポリエーテル
系、ポリアミド系等の有機化合物系にした吸収冷凍装置
。(3) An absorption refrigeration apparatus in which an evaporator, an absorber, and a concentrating section are connected by a pipe to constitute a refrigeration cycle, and the means for concentrating the diluted absorption liquid in the concentrating section is a concentrating means by reverse osmosis, wherein the concentration An absorption refrigeration device whose semipermeable membrane is made of an organic compound such as cellulose, polyether, or polyamide.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP12010489A JPH02298767A (en) | 1989-05-12 | 1989-05-12 | Absorption refrigerator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP12010489A JPH02298767A (en) | 1989-05-12 | 1989-05-12 | Absorption refrigerator |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH02298767A true JPH02298767A (en) | 1990-12-11 |
Family
ID=14778026
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP12010489A Pending JPH02298767A (en) | 1989-05-12 | 1989-05-12 | Absorption refrigerator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH02298767A (en) |
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2088389A1 (en) * | 2008-02-05 | 2009-08-12 | Evonik Degussa GmbH | Absorption cooling machine |
| US8069687B2 (en) | 2005-06-17 | 2011-12-06 | Evonik Degussa Gmbh | Working media for refrigeration processes |
| JP2013529280A (en) * | 2010-04-20 | 2013-07-18 | エボニック デグサ ゲーエムベーハー | Absorption heat pump having an absorbent containing lithium chloride and an organic chloride salt |
| US8500867B2 (en) | 2009-02-02 | 2013-08-06 | Evonik Degussa Gmbh | CO2 absorption from gas mixtures using an aqueous solution of 4-amino-2,2,6,6-tetramethylpiperidine |
| US8696928B2 (en) | 2009-12-07 | 2014-04-15 | Evonik Degussa Gmbh | Operating medium for an absorption refrigeration device |
| US8784537B2 (en) | 2010-11-12 | 2014-07-22 | Evonik Degussa Gmbh | Amine-containing absorption medium, process and apparatus for absorption of acidic gases from gas mixtures |
| US8932478B2 (en) | 2008-02-05 | 2015-01-13 | Evonik Degussa Gmbh | Process for the absorption of a volatile substance in a liquid absorbent |
| US9221007B2 (en) | 2011-11-14 | 2015-12-29 | Evonik Degussa Gmbh | Method and device for separating acid gases from a gas mixture |
| US9630140B2 (en) | 2012-05-07 | 2017-04-25 | Evonik Degussa Gmbh | Method for absorbing CO2 from a gas mixture |
| US9840473B1 (en) | 2016-06-14 | 2017-12-12 | Evonik Degussa Gmbh | Method of preparing a high purity imidazolium salt |
| US9878285B2 (en) | 2012-01-23 | 2018-01-30 | Evonik Degussa Gmbh | Method and absorption medium for absorbing CO2 from a gas mixture |
| US10105644B2 (en) | 2016-06-14 | 2018-10-23 | Evonik Degussa Gmbh | Process and absorbent for dehumidifying moist gas mixtures |
| US10138209B2 (en) | 2016-06-14 | 2018-11-27 | Evonik Degussa Gmbh | Process for purifying an ionic liquid |
| US10493400B2 (en) | 2016-06-14 | 2019-12-03 | Evonik Degussa Gmbh | Process for dehumidifying moist gas mixtures |
| US10500540B2 (en) | 2015-07-08 | 2019-12-10 | Evonik Degussa Gmbh | Method for dehumidifying humid gas mixtures using ionic liquids |
| US10512881B2 (en) | 2016-06-14 | 2019-12-24 | Evonik Degussa Gmbh | Process for dehumidifying moist gas mixtures |
| US10512883B2 (en) | 2016-06-14 | 2019-12-24 | Evonik Degussa Gmbh | Process for dehumidifying moist gas mixtures |
-
1989
- 1989-05-12 JP JP12010489A patent/JPH02298767A/en active Pending
Cited By (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8069687B2 (en) | 2005-06-17 | 2011-12-06 | Evonik Degussa Gmbh | Working media for refrigeration processes |
| EP2088389A1 (en) * | 2008-02-05 | 2009-08-12 | Evonik Degussa GmbH | Absorption cooling machine |
| WO2009098155A1 (en) * | 2008-02-05 | 2009-08-13 | Evonik Degussa Gmbh | Absorption type refrigerating machine |
| US8932478B2 (en) | 2008-02-05 | 2015-01-13 | Evonik Degussa Gmbh | Process for the absorption of a volatile substance in a liquid absorbent |
| US8500867B2 (en) | 2009-02-02 | 2013-08-06 | Evonik Degussa Gmbh | CO2 absorption from gas mixtures using an aqueous solution of 4-amino-2,2,6,6-tetramethylpiperidine |
| US8500892B2 (en) | 2009-02-02 | 2013-08-06 | Evonik Degussa Gmbh | CO2 absorption from gas mixtures using an aqueous solution of 4-amino-2,2,6,6-tetramethylpiperidine |
| US8623123B2 (en) | 2009-02-02 | 2014-01-07 | Evonik Degussa Gmbh | CO2 absorption from gas mixtures using an aqueous solution of 4-amino-2,2,6,6-tetramethyl piperidine |
| US8696928B2 (en) | 2009-12-07 | 2014-04-15 | Evonik Degussa Gmbh | Operating medium for an absorption refrigeration device |
| JP2013529280A (en) * | 2010-04-20 | 2013-07-18 | エボニック デグサ ゲーエムベーハー | Absorption heat pump having an absorbent containing lithium chloride and an organic chloride salt |
| US8784537B2 (en) | 2010-11-12 | 2014-07-22 | Evonik Degussa Gmbh | Amine-containing absorption medium, process and apparatus for absorption of acidic gases from gas mixtures |
| US9221007B2 (en) | 2011-11-14 | 2015-12-29 | Evonik Degussa Gmbh | Method and device for separating acid gases from a gas mixture |
| US9878285B2 (en) | 2012-01-23 | 2018-01-30 | Evonik Degussa Gmbh | Method and absorption medium for absorbing CO2 from a gas mixture |
| US9630140B2 (en) | 2012-05-07 | 2017-04-25 | Evonik Degussa Gmbh | Method for absorbing CO2 from a gas mixture |
| US10500540B2 (en) | 2015-07-08 | 2019-12-10 | Evonik Degussa Gmbh | Method for dehumidifying humid gas mixtures using ionic liquids |
| US9840473B1 (en) | 2016-06-14 | 2017-12-12 | Evonik Degussa Gmbh | Method of preparing a high purity imidazolium salt |
| US10105644B2 (en) | 2016-06-14 | 2018-10-23 | Evonik Degussa Gmbh | Process and absorbent for dehumidifying moist gas mixtures |
| US10138209B2 (en) | 2016-06-14 | 2018-11-27 | Evonik Degussa Gmbh | Process for purifying an ionic liquid |
| US10493400B2 (en) | 2016-06-14 | 2019-12-03 | Evonik Degussa Gmbh | Process for dehumidifying moist gas mixtures |
| US10512881B2 (en) | 2016-06-14 | 2019-12-24 | Evonik Degussa Gmbh | Process for dehumidifying moist gas mixtures |
| US10512883B2 (en) | 2016-06-14 | 2019-12-24 | Evonik Degussa Gmbh | Process for dehumidifying moist gas mixtures |
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