JPH0331087B2 - - Google Patents
Info
- Publication number
- JPH0331087B2 JPH0331087B2 JP61034107A JP3410786A JPH0331087B2 JP H0331087 B2 JPH0331087 B2 JP H0331087B2 JP 61034107 A JP61034107 A JP 61034107A JP 3410786 A JP3410786 A JP 3410786A JP H0331087 B2 JPH0331087 B2 JP H0331087B2
- Authority
- JP
- Japan
- Prior art keywords
- carbon monoxide
- heat pump
- refrigerant
- condenser
- liquefied
- 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.)
- Expired - Lifetime
Links
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 44
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 44
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 28
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 23
- 238000004821 distillation Methods 0.000 claims description 19
- 239000007789 gas Substances 0.000 claims description 18
- 239000003507 refrigerant Substances 0.000 claims description 18
- 229910052757 nitrogen Inorganic materials 0.000 claims description 10
- 238000011084 recovery Methods 0.000 claims description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 9
- 229910052799 carbon Inorganic materials 0.000 claims description 9
- 230000006835 compression Effects 0.000 claims description 8
- 238000007906 compression Methods 0.000 claims description 8
- 239000003949 liquefied natural gas Substances 0.000 claims description 7
- 238000010992 reflux Methods 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 5
- 239000002994 raw material Substances 0.000 claims description 4
- 238000001704 evaporation Methods 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 2
- 229910001873 dinitrogen Inorganic materials 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 239000000700 radioactive tracer Substances 0.000 description 1
Classifications
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Carbon And Carbon Compounds (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、原料としての一酸化炭素の供給路に
接続した蒸留塔の上部に、一酸化炭素ガスを冷却
して液化一酸化炭素を還流するコンデンサーを接
続し、液化一酸化炭素を加熱して一酸化炭素ガス
を還流する加熱器を前記蒸留塔の下部に接続し、
重炭素から成る一酸化炭素の少ない一酸化炭素ガ
スの回収路を前記コンデンサーに接続し、重炭素
から成る一酸化炭素の多い液化一酸化炭素の回収
路を前記加熱器に接続した重炭素から成る一酸化
炭素の分離装置、詳しくはコンデンサーの改良に
関する。[Detailed Description of the Invention] [Industrial Application Field] The present invention cools carbon monoxide gas and refluxes liquefied carbon monoxide into the upper part of a distillation column connected to a supply line for carbon monoxide as a raw material. A condenser is connected to the bottom of the distillation column, and a heater for heating liquefied carbon monoxide and refluxing carbon monoxide gas is connected to the bottom of the distillation column.
A recovery channel for carbon monoxide gas containing heavy carbon with a low amount of carbon monoxide is connected to the condenser, and a recovery channel for liquefied carbon monoxide gas containing heavy carbon and containing a large amount of carbon monoxide is connected to the heater. This article relates to carbon monoxide separation equipment, specifically to improvements in condensers.
従来、コンデンサーの冷却管に、一酸化炭素ガ
スの凝縮に必要な極低温の液体窒素を直接供給し
ていた。
Conventionally, the cryogenic liquid nitrogen needed to condense carbon monoxide gas was directly supplied to the condenser cooling tube.
しかし、コンデンサーにおいて大量の窒素ガス
が発生し、窒素ガスを大量に必要とする需要先が
一般には無いため、コンデンサーからの窒素ガス
を放出しなければならず、液体窒素の消費に起因
して運転経費が膨大になる欠点があつた。
However, a large amount of nitrogen gas is generated in the condenser, and since there is generally no customer that requires a large amount of nitrogen gas, the nitrogen gas from the condenser must be released, and the operation may be interrupted due to the consumption of liquid nitrogen. The drawback was that the costs were enormous.
本発明の目的は、コンデンサーによる一酸化炭
素ガスの冷却に要する経費を大幅に少なくできる
ようにする点にある。 An object of the present invention is to significantly reduce the cost required for cooling carbon monoxide gas using a condenser.
本発明の特徴構成は、蒸留塔からの一酸化炭素
ガスを凝縮して液化一酸化炭素を還流するための
コンデンサーが、窒素を冷媒とする圧縮式第１ヒ
ートポンプの蒸発器と一体成形され、その第１ヒ
ートポンプの放熱器と、メタンを冷媒とする圧縮
式第２ヒートポンプの蒸発器とが、冷媒メタンの
加熱蒸発で冷媒窒素が冷却凝縮されるように兼用
形成され、その第２ヒートポンプの放熱器が、液
化天然ガスによつてメタン冷媒を冷却する熱交換
器であることにあり、その作用効果は次の通りで
ある。
A characteristic configuration of the present invention is that a condenser for condensing carbon monoxide gas from a distillation column and refluxing liquefied carbon monoxide is integrally formed with an evaporator of a compression type first heat pump using nitrogen as a refrigerant. The radiator of the first heat pump and the evaporator of the second compression type heat pump using methane as a refrigerant are formed so that the refrigerant nitrogen is cooled and condensed by heating and evaporating the refrigerant methane, and the radiator of the second heat pump is a heat exchanger that cools methane refrigerant with liquefied natural gas, and its functions and effects are as follows.
つまり、コンデンサー内の一酸化炭素ガスは約
0.8ata、−193℃である。他方、10ata、−150℃の
液化天然ガス（LNG）を第２ヒートポンプの冷
熱源として第１及び第２ヒートポンプを運転し、
第１ヒートポンプの冷媒として窒素を、かつ、第
２ヒートポンプの冷媒としてメタンを利用する
と、第２ヒートポンプの蒸発器に約1ata、−160℃
の液化メタンを供給でき、かつ、第１ヒートポン
プの蒸発器に約0.6ata、−200℃の液化窒素を供給
でき、コンデンサー内の一酸化炭素ガスを第１ヒ
ートポンプの蒸発器によつて十分に冷却凝縮でき
る。
In other words, the carbon monoxide gas in the condenser is approximately
0.8ata, -193℃. On the other hand, the first and second heat pumps are operated using 10ata, -150℃ liquefied natural gas (LNG) as a cold heat source for the second heat pump,
When nitrogen is used as the refrigerant in the first heat pump and methane is used as the refrigerant in the second heat pump, the temperature in the evaporator of the second heat pump is approximately 1 ata, -160°C.
It is possible to supply approximately 0.6ata of liquefied nitrogen at -200℃ to the evaporator of the first heat pump, and the carbon monoxide gas in the condenser is sufficiently cooled by the evaporator of the first heat pump. Can be condensed.
また、第２ヒートポンプの放熱器からの天然ガ
ス（NG）は、燃料等として大量の需要があり、
放出せずに有価物として回収利用でき、LNGを
無駄にしないで、コンデンサーでの一酸化炭素ガ
スの冷却凝縮をトータルコストとして大幅に経費
節減した状態で行える。 In addition, there is a large demand for natural gas (NG) from the radiator of the second heat pump as fuel, etc.
It can be recovered and reused as a valuable resource without being released, and without wasting LNG, it is possible to cool and condense carbon monoxide gas in a condenser with a significant reduction in total cost.
その結果、同位元素検査のトレーサ等に有用な
原子量が13の炭素から成る一酸化炭素を、製造コ
ストを大幅に低減して安価提供できるようになつ
た。
As a result, carbon monoxide, which is composed of carbon with an atomic weight of 13 and is useful as a tracer for isotope testing, can now be provided at a low price by significantly reducing manufacturing costs.
次に第１図により実施例を示す。 Next, an example will be shown with reference to FIG.
蒸留塔１に原料としての一酸化炭素の供給路２
を接続し、蒸留塔１からの重炭素から成る一酸化
炭素の少ない一酸化炭素ガスを冷却して液化一酸
化炭素を蒸留塔１に還流するコンデンサー３を、
蒸留塔１の上部に接続し、重炭素から成る一酸化
炭素の少ない一酸化炭素ガスの回収路４をコンデ
ンサー３に接続してある。 Supply path 2 for carbon monoxide as a raw material to the distillation column 1
A condenser 3 is connected to the condenser 3 which cools the carbon monoxide gas containing less carbon monoxide consisting of heavy carbon from the distillation column 1 and refluxes liquefied carbon monoxide to the distillation column 1.
A condenser 3 is connected to the upper part of the distillation column 1, and a recovery path 4 for collecting carbon monoxide gas, which is composed of heavy carbon and has little carbon monoxide, is connected to the condenser 3.
圧縮機５、放熱器６、減圧弁７、蒸発器８の順
に冷媒としての窒素を循環させる圧縮式第１ヒー
トポンプＡを設け、その蒸発器８をコンデンサー
３と一体成形してある。 A first compression heat pump A is provided that circulates nitrogen as a refrigerant in the order of a compressor 5, a radiator 6, a pressure reducing valve 7, and an evaporator 8, and the evaporator 8 is integrally molded with the condenser 3.
圧縮機１１、放熱器１２、減圧弁１３、蒸発器
１４の順に冷媒としてのメタンを循環させる圧縮
式第２ヒートポンプＢを設け、第２ヒートポンプ
Ｂの蒸発器１４と第１ヒートポンプＡの放熱器６
を、冷媒メタンの加熱蒸発で冷媒窒素が冷却凝縮
されるように兼用形成してあり、また、第２ヒー
トポンプＢの放熱器１２は、冷却管１２ａの
LNGによつてメタン冷媒を冷却する熱交換器か
ら成り、その放熱器１２からのNGを回収するガ
スホルダーを設けてある。 A compression type second heat pump B is provided that circulates methane as a refrigerant in the order of the compressor 11, radiator 12, pressure reducing valve 13, and evaporator 14, and the evaporator 14 of the second heat pump B and the radiator 6 of the first heat pump A are provided.
is formed so that the refrigerant nitrogen is cooled and condensed by heating evaporation of the refrigerant methane, and the radiator 12 of the second heat pump B is connected to the cooling pipe 12a.
It consists of a heat exchanger that cools methane refrigerant with LNG, and is provided with a gas holder that collects NG from the radiator 12.
蒸留塔１からの重炭素から成る一酸化炭素の多
い液化一酸化炭素を加熱して一酸化炭素ガスを蒸
留塔１に還流する加熱器９を、蒸留塔１の下部に
接続し、重炭素から成る一酸化炭素の多い液化一
酸化炭素の回収路１０を加熱器９に接続してあ
る。加熱器９の加熱管９ａは、液状炭化水素系の
熱搬送媒体により液化一酸化炭素を気化させるも
のである。 A heater 9 is connected to the lower part of the distillation column 1 and heats the liquefied carbon monoxide containing a large amount of carbon monoxide, which is made up of heavy carbon, from the distillation column 1 and refluxes carbon monoxide gas to the distillation column 1. A recovery path 10 for liquefied carbon monoxide containing a large amount of carbon monoxide is connected to a heater 9. The heating tube 9a of the heater 9 vaporizes liquefied carbon monoxide using a liquid hydrocarbon-based heat transfer medium.
次に別実施例を説明する。 Next, another embodiment will be described.
蒸留塔１の具体構成は、例えば多段塔型式や充
填塔型式、その他適宜変更が可能であり、また、
複数又は多数の蒸留塔１を多段式に接続して、つ
まり回収路１０を後段の蒸留塔１にかつ回収路４
を前段の蒸留塔１に接続して設置してもよい。 The specific configuration of the distillation column 1 can be changed as appropriate, such as a multi-stage column type or a packed column type, and
A plurality or a large number of distillation columns 1 are connected in a multi-stage manner, that is, the recovery passage 10 is connected to the subsequent distillation column 1 and the recovery passage 4 is connected to the distillation column 1 in the latter stage.
may be installed by being connected to the distillation column 1 in the preceding stage.
コンデンサー３や加熱器９の型式は適当に変更
できる。 The models of the condenser 3 and heater 9 can be changed as appropriate.
圧縮式第１及び第２ヒートポンプＡ，Ｂの具体
構成は適当に変更できる。例えば、圧縮機５，１
１を遠心型、軸流型、ピストン型等にしたり、あ
るいは、第２図に示すように、第２ヒートポンプ
Ｂにおいて、第１圧縮機１１ａ、冷媒メタン冷却
部１１ｂ、第２圧縮機１１ｃから成る圧縮手段１
１を設け、冷媒メタン冷却部１１ｂと放熱部１２
をLNG供給管１５で接続し、第２ヒートポンプ
Ｂでの必要動力量を少なくできるようにしてもよ
い。 The specific configurations of the first and second compression heat pumps A and B can be changed as appropriate. For example, compressor 5,1
1 may be of a centrifugal type, an axial flow type, a piston type, etc., or, as shown in FIG. Compression means 1
1 is provided, and a refrigerant methane cooling section 11b and a heat radiation section 12 are provided.
may be connected by an LNG supply pipe 15 to reduce the amount of power required by the second heat pump B.
第１図は本発明の実施例を示すフローシート、
第２図は本発明の別実施例を示すフローシートで
ある。
１……蒸留塔、２……原料としての一酸化炭素
の供給路、３……コンデンサー、４……一酸化炭
素ガスの回収路、６……第１ヒートポンプの放熱
器、８……第１ヒートポンプの蒸発器、９……加
熱器、１０……液化一酸化炭素の回収路、１２…
…第２ヒートポンプの放熱器、１４……第２ヒー
トポンプの蒸発器、Ａ……第１ヒートポンプ、Ｂ
……第２ヒートポンプ。
FIG. 1 is a flow sheet showing an embodiment of the present invention;
FIG. 2 is a flow sheet showing another embodiment of the present invention. 1... Distillation column, 2... Supply path for carbon monoxide as a raw material, 3... Condenser, 4... Recovery path for carbon monoxide gas, 6... Heat radiator of the first heat pump, 8... First Heat pump evaporator, 9... Heater, 10... Liquefied carbon monoxide recovery path, 12...
...Radiator of second heat pump, 14...Evaporator of second heat pump, A...First heat pump, B
...Second heat pump.
Claims (1)
た蒸留塔１の上部に、一酸化炭素ガスを冷却して
液化一酸化炭素を還流するコンデンサー３を接続
し、液化一酸化炭素を加熱して一酸化炭素ガスを
還流する加熱器９を前記蒸留塔１の下部に接続
し、重炭素から成る一酸化炭素の少ない一酸化炭
素ガスの回収路４を前記コンデンサー３に接続
し、重炭素から成る一酸化炭素の多い液化一酸化
炭素の回収路１０を前記加熱器９に接続した重炭
素から成る一酸化炭素の分離装置であつて、前記
コンデンサー３が、窒素を冷媒とする圧縮式第１
ヒートポンプＡの蒸発器８と一体成形され、その
第１ヒートポンプＡの放熱器６と、メタンを冷媒
とする圧縮式第２ヒートポンプＢの蒸発器１４と
が、冷媒メタンの加熱蒸発で冷媒窒素が冷却凝縮
されるように兼用形成され、その第２ヒートポン
プＢの放熱器１２が、液化天然ガスによつてメタ
ン冷媒を冷却する熱交換器である重炭素から成る
一酸化炭素の分離装置。1. A condenser 3 for cooling carbon monoxide gas and refluxing liquefied carbon monoxide is connected to the upper part of a distillation column 1 connected to a supply line 2 for carbon monoxide as a raw material, and the liquefied carbon monoxide is heated and A heater 9 for refluxing carbon monoxide gas is connected to the lower part of the distillation column 1, and a recovery path 4 for carbon monoxide gas containing heavy carbon and containing less carbon monoxide is connected to the condenser 3. This is a carbon monoxide separation device made of heavy carbon, in which a recovery path 10 for liquefied carbon monoxide containing a large amount of carbon monoxide is connected to the heater 9, and the condenser 3 is a first compression type condenser using nitrogen as a refrigerant.
The radiator 6 of the first heat pump A, which is integrally formed with the evaporator 8 of the heat pump A, and the evaporator 14 of the compression type second heat pump B, which uses methane as a refrigerant, cool the refrigerant nitrogen by heating and evaporating the refrigerant methane. A device for separating carbon monoxide consisting of heavy carbon, which is also formed to be condensed and whose radiator 12 of the second heat pump B is a heat exchanger for cooling a methane refrigerant by means of liquefied natural gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61034107A JPS62191030A (en) | 1986-02-18 | 1986-02-18 | Apparatus for separating carbon monoxide comprising heavy carbon |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61034107A JPS62191030A (en) | 1986-02-18 | 1986-02-18 | Apparatus for separating carbon monoxide comprising heavy carbon |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS62191030A JPS62191030A (en) | 1987-08-21 |
| JPH0331087B2 true JPH0331087B2 (en) | 1991-05-02 |
Family
ID=12405050
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61034107A Granted JPS62191030A (en) | 1986-02-18 | 1986-02-18 | Apparatus for separating carbon monoxide comprising heavy carbon |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS62191030A (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2512360B (en) | 2013-03-27 | 2015-08-05 | Highview Entpr Ltd | Method and apparatus in a cryogenic liquefaction process |
-
1986
- 1986-02-18 JP JP61034107A patent/JPS62191030A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS62191030A (en) | 1987-08-21 |
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