JPS6150239B2 - - Google Patents
Info
- Publication number
- JPS6150239B2 JPS6150239B2 JP54083970A JP8397079A JPS6150239B2 JP S6150239 B2 JPS6150239 B2 JP S6150239B2 JP 54083970 A JP54083970 A JP 54083970A JP 8397079 A JP8397079 A JP 8397079A JP S6150239 B2 JPS6150239 B2 JP S6150239B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- carbon monoxide
- hydrogen
- conduit
- methane
- 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
Links
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 32
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 31
- 239000007788 liquid Substances 0.000 claims description 31
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 30
- 239000007789 gas Substances 0.000 claims description 29
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 19
- 229910052739 hydrogen Inorganic materials 0.000 claims description 16
- 239000001257 hydrogen Substances 0.000 claims description 16
- 239000002994 raw material Substances 0.000 claims description 12
- 238000000034 method Methods 0.000 claims description 6
- 238000000629 steam reforming Methods 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims 1
- 229910052799 carbon Inorganic materials 0.000 claims 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 claims 1
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
Description
【発明の詳細な説明】
本発明は、深冷分離により水素，一酸化炭素を
分離するもので、特にスチームリホーミングガス
よりの深冷分離法による水素，一酸化炭素の分離
方法に関するものである。[Detailed Description of the Invention] The present invention is for separating hydrogen and carbon monoxide by cryogenic separation, and particularly relates to a method for separating hydrogen and carbon monoxide from steam reforming gas by cryogenic separation. .
従来のスチームリホーミングガスより水素，一
酸化炭素を深冷分離する方法では、原料ガスと一
酸化炭素とメタンを分離する精留塔塔底液との熱
交換は、塔底液中のメタン濃度が高い程蒸発温度
が高くなり、原料ガスの冷却曲線と塔底液の蒸発
曲線が近接し、原料ガスと塔底液の温度差が小さ
くなるので熱交換が難しくなる。それを解決する
ために塔底液中のメタン濃度を下げ、一酸化炭素
の濃度を高くすることにより、塔底液の蒸発曲線
を低温にする方法が採用されている。しかしなが
ら、この方法によると、塔底液中の一酸化炭素濃
度を高くするため、搭頂よりの製品となる一酸化
炭素量が減少し、回収率が下がるため原単位が低
下するという欠点があつた。 In the conventional cryogenic separation method of hydrogen and carbon monoxide from steam reforming gas, heat exchange between the raw material gas and the bottom liquid of the rectification column that separates carbon monoxide and methane is performed to reduce the methane concentration in the bottom liquid. The higher the value, the higher the evaporation temperature, the closer the cooling curve of the raw material gas is to the evaporation curve of the bottom liquid, and the smaller the temperature difference between the raw material gas and the bottom liquid, making heat exchange difficult. To solve this problem, a method has been adopted in which the evaporation curve of the tower bottom liquid is lowered by lowering the methane concentration and increasing the carbon monoxide concentration in the tower bottom liquid. However, this method has the drawback of increasing the carbon monoxide concentration in the bottom liquid, which reduces the amount of carbon monoxide that becomes a product from the top of the tower, lowering the recovery rate and lowering the basic unit. Ta.
本発明は、スチームリホーミングガスより水
素，一酸化炭素を深冷分離する方法において、従
来行なわれている方法よりも設備費を増大させる
ことなく、容易に製品となる一酸化炭素の回収率
を高くして、装置の原単位を低下させることを目
的としたものである。 The present invention is a method for cryogenically separating hydrogen and carbon monoxide from steam reforming gas, and the present invention improves the recovery rate of carbon monoxide, which can be easily turned into products, without increasing equipment costs compared to conventional methods. The purpose is to increase the energy consumption and reduce the unit consumption of the device.
本発明は、精留塔の塔底温度を高くすることに
より、塔底液中の一酸化炭素の濃度を低くして、
搭頂より製品一酸化炭素量を増大させると共に、
水素タービン出口の水素ガスの一部を精留塔底部
より抜き出した塔底液と調節混合することによ
り、塔底液のメタン分圧を下げて原料ガスとの熱
交換に必要とする温度差を得るようにしたもので
ある。 The present invention lowers the concentration of carbon monoxide in the bottom liquid by increasing the bottom temperature of the rectification column.
In addition to increasing the amount of carbon monoxide in the product from the top,
By adjusting and mixing a portion of the hydrogen gas at the hydrogen turbine outlet with the bottom liquid extracted from the bottom of the rectification tower, the methane partial pressure of the bottom liquid is lowered and the temperature difference required for heat exchange with the raw gas is reduced. It was designed to be obtained.
以下、本発明の一実施例を図面によつて説明す
ると、スチームリホーミングガスは水分，炭酸ガ
ス等の低温において凝固する成分を除去したの
ち、深冷分離装置の原料ガスとして導管１４より
保冷槽８に入り、熱交換器１において低温戻りガ
スの寒冷により冷却され、導管１５より気液分離
器２に入る。気液分離器２において分離された一
酸化炭素およびメタンを主成分とし、水素を微量
含む凝縮液は、導管１６より膨脹弁９によつて膨
脹し、導管１７よりフラツシユドラム３に入り、
ここで膨脹により気化した水素ガスは導管３６、
熱交換器１を経て導管３７よりフラツシユガスと
して取り出され、燃料等に使用される。一方、フ
ラツシユドラム３内の一酸化炭素およびメタンの
混合液は、導管１８、弁１０、熱交換器１を通つ
て精留塔４の供給原料として導管１９より供給さ
れる。精留塔４では、搭頂より高純度の一酸化炭
素が得られ、導管２０より熱交換器１にて原料ガ
スを冷却し、温度回復したのち導管２１を通つて
圧縮機７にて所定の圧力まで昇圧され、導管２
２，２３より製品の一酸化炭素として取り出され
る。導管２４により分岐された一部の一酸化炭素
は、精留塔リボイラ５の熱源として利用するとと
もに、精留塔４の環流液として利用するもので、
導管２４より熱交換器１において低温戻りガスの
寒冷により冷却された後導管２５よりリボイラ５
に入り、精留塔４を加熱するため一酸化炭素は液
化され、導管２６、弁１３より精留塔４に送ら
れ、環流液として使用される。また、精留塔４の
塔底液はリボイラ５によつて加熱されるため、塔
底液中の一酸化炭素濃度は低くなり、搭頂よりの
製品一酸化炭素量は増大する。気液分離器２にお
いて分離された水素を主成分とした非凝縮ガス
は、導管２７より熱交換器１にて所定の温度まで
昇温され、水素タービン６にて膨脹しガスを低下
させて導管２９より一部は導管３０を経て再び熱
交換器１に入り、原料ガスと熱交換して温度回復
した後導管３１より水素ガスとして送出される。
水素タービン６出口の水素ガスの一部は、導管３
２、弁１１を通り、導管３３，弁１２を通つて抜
き出された精留塔４の塔底液と合流して塔底液の
メタン分圧を下げ、導管３４より熱交換器１にて
原料ガスと熱交換して温度回復した後、オフガス
として導管３５より取り出される。この場合、弁
１１により塔底液に混合される水素ガス量を調節
することにより、塔底液のメタン分圧を任意に低
下させることができ、原料ガスとの熱交換に必要
な温度差を確保することができる。 Hereinafter, one embodiment of the present invention will be described with reference to the drawings. After removing components that solidify at low temperatures, such as moisture and carbon dioxide, steam reforming gas is passed through a conduit 14 to a cold storage tank as a raw material gas for a cryogenic separation device. 8, is cooled by the cold return gas in the heat exchanger 1, and enters the gas-liquid separator 2 through the conduit 15. The condensate, which is separated in the gas-liquid separator 2 and whose main components are carbon monoxide and methane and contains a small amount of hydrogen, is expanded through the expansion valve 9 through the conduit 16, enters the flash drum 3 through the conduit 17,
Here, the hydrogen gas vaporized by expansion is transferred to a conduit 36,
It passes through the heat exchanger 1 and is taken out as flash gas from the conduit 37, and is used as fuel or the like. On the other hand, the mixture of carbon monoxide and methane in the flash drum 3 passes through the conduit 18, the valve 10, and the heat exchanger 1, and is supplied from the conduit 19 as a feedstock to the rectification column 4. In the rectification column 4, high-purity carbon monoxide is obtained from the top, and the raw material gas is cooled in the heat exchanger 1 through the conduit 20, and after the temperature has been recovered, it is passed through the conduit 21 into the compressor 7 to a predetermined level. The pressure is increased to the pressure of conduit 2.
2,23, it is extracted as carbon monoxide from the product. A part of the carbon monoxide branched off by the conduit 24 is used as a heat source for the rectification tower reboiler 5 and as a reflux liquid of the rectification tower 4.
The low-temperature return gas is cooled in the heat exchanger 1 through the conduit 24 and then sent through the reboiler 5 through the conduit 25.
The carbon monoxide enters the rectification column 4 and is liquefied to heat the rectification column 4, and is sent to the rectification column 4 through the conduit 26 and valve 13, where it is used as a reflux liquid. Further, since the bottom liquid of the rectification column 4 is heated by the reboiler 5, the concentration of carbon monoxide in the bottom liquid becomes low, and the amount of carbon monoxide product from the top of the column increases. The non-condensable gas mainly composed of hydrogen separated in the gas-liquid separator 2 is heated through the conduit 27 to a predetermined temperature in the heat exchanger 1, and expanded in the hydrogen turbine 6 to lower the gas and sent to the conduit. A portion of the hydrogen from 29 enters the heat exchanger 1 again through the conduit 30, and after exchanging heat with the raw material gas to recover the temperature, is sent out through the conduit 31 as hydrogen gas.
A portion of the hydrogen gas at the outlet of the hydrogen turbine 6 is transferred to the conduit 3
2. It passes through the valve 11, joins with the bottom liquid of the rectification column 4 extracted through the conduit 33 and the valve 12, lowers the partial pressure of methane in the bottom liquid, and passes through the conduit 34 into the heat exchanger 1. After recovering the temperature by exchanging heat with the raw material gas, it is taken out from the conduit 35 as an off-gas. In this case, by adjusting the amount of hydrogen gas mixed into the tower bottom liquid using the valve 11, the methane partial pressure of the tower bottom liquid can be lowered arbitrarily, and the temperature difference required for heat exchange with the raw material gas can be reduced. can be secured.
精留塔４では塔頂より一酸化炭素、塔底よりメ
タンを主成分とする一酸化炭素を含む混合液が抜
き出されており、精留塔４の塔底温度を下げると
塔底液中の一酸化炭素の濃度が高くなり、塔頂よ
りの一酸化炭素が減少して回収率が低下する。し
かして、精留塔４の塔底温度を下げることは、塔
底液中の一酸化炭素の濃度が高くなり、メタンの
濃度が低下してメタン分圧を下げることになるた
め、従来の方法では塔底液の蒸発温度を下げて熱
交換器１での原料ガスとの温度差を得ているが、
本発明は精留塔４の塔底温度を高くし、塔底液中
の一酸化炭素濃度を低くして塔頂よりの製品一酸
化炭素量を増大させると共に、水素タービン６出
口の水素ガスの一部を精留塔底部より抜出した塔
底液と調節混合して、塔底液のメタン分圧を下げ
ることにより、原料ガスとの熱交換に必要な温度
差を得ることができる。 In the rectifying column 4, carbon monoxide is extracted from the top of the column, and a mixed liquid containing carbon monoxide whose main component is methane is extracted from the bottom of the column. The concentration of carbon monoxide increases, the amount of carbon monoxide at the top of the column decreases, and the recovery rate decreases. However, lowering the bottom temperature of the rectification column 4 increases the concentration of carbon monoxide in the bottom liquid, which reduces the concentration of methane and lowers the partial pressure of methane. In this case, the evaporation temperature of the tower bottom liquid is lowered to obtain a temperature difference with the raw material gas in heat exchanger 1.
The present invention increases the temperature at the bottom of the rectifying column 4 and lowers the concentration of carbon monoxide in the bottom liquid to increase the amount of carbon monoxide product from the top of the column. By adjusting and mixing a portion with the bottom liquid extracted from the bottom of the rectification column to lower the methane partial pressure of the bottom liquid, it is possible to obtain the temperature difference necessary for heat exchange with the raw material gas.
本発明は以上述べたようにしたものであるか
ら、設備費を増大させることなく製品一酸化炭素
の回収率を増大させることができ、装置の原単位
を低下させることができる。 Since the present invention is as described above, it is possible to increase the recovery rate of product carbon monoxide without increasing equipment costs, and it is possible to reduce the unit consumption of the device.
図面は本発明によるスチームリホーミングガス
より水素、一酸化炭素を深冷分離する方法を実施
した装置の一例を示す系統図である。
１……熱交換器、２……気液分離器、３……フ
ラツシユドラム、４……精留塔、５……リボイ
ラ、６……水素タービン、７……圧縮機、８……
保冷槽、９〜１３……弁、１４〜３７……導管。
The drawing is a system diagram showing an example of an apparatus implementing the method of cryogenically separating hydrogen and carbon monoxide from steam reforming gas according to the present invention. 1... heat exchanger, 2... gas-liquid separator, 3... flash drum, 4... rectification column, 5... reboiler, 6... hydrogen turbine, 7... compressor, 8...
Cold storage tank, 9-13... Valve, 14-37... Conduit.
Claims (1)
した後水素を主成分とする非凝縮ガスと一酸化炭
素およびメタンを含む凝縮液とに気液分離し、該
凝縮液をフラツシユさせて一酸化炭素とメタンの
混合液を精留塔に導入し、該精留塔の塔頂より一
酸化炭素を抜出すと共に精留塔の塔底よりメタン
を主成分とする塔底液を抜出し、前記水素を主成
分とする非凝縮ガスを水素タービンに導入し、該
水素タービン出口の水素ガスの一部を前記塔底液
に調節混合して原料ガスとの熱交換に必要な温度
差を得ることを特徴とするスチームリホーミング
ガスより水素，一酸化炭素を深冷分離する方法。1 After cooling the raw material gas by heat exchange with the low-temperature return gas, it is separated into gas and liquid into a non-condensable gas whose main component is hydrogen and a condensate containing carbon monoxide and methane, and the condensate is flashed to produce monoxide. A mixture of carbon and methane is introduced into a rectification column, carbon monoxide is extracted from the top of the rectification column, and a bottom liquid containing methane as a main component is extracted from the bottom of the rectification column. A non-condensable gas mainly composed of is introduced into a hydrogen turbine, and a part of the hydrogen gas at the outlet of the hydrogen turbine is adjusted and mixed with the bottom liquid to obtain a temperature difference necessary for heat exchange with the raw material gas. A method of cryogenically separating hydrogen and carbon monoxide from steam reforming gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP8397079A JPS5610681A (en) | 1979-07-04 | 1979-07-04 | Deeppfreezing method of separating hydrogen and carbon monoxide from steam reforming gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP8397079A JPS5610681A (en) | 1979-07-04 | 1979-07-04 | Deeppfreezing method of separating hydrogen and carbon monoxide from steam reforming gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5610681A JPS5610681A (en) | 1981-02-03 |
| JPS6150239B2 true JPS6150239B2 (en) | 1986-11-01 |
Family
ID=13817389
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP8397079A Granted JPS5610681A (en) | 1979-07-04 | 1979-07-04 | Deeppfreezing method of separating hydrogen and carbon monoxide from steam reforming gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5610681A (en) |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5325294A (en) * | 1976-08-20 | 1978-03-08 | Hitachi Ltd | Separating method for carbon monoxide gas |
| JPS5339289A (en) * | 1976-09-22 | 1978-04-11 | Hitachi Ltd | Separating method for carbon monoxide |
-
1979
- 1979-07-04 JP JP8397079A patent/JPS5610681A/en active Granted
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5325294A (en) * | 1976-08-20 | 1978-03-08 | Hitachi Ltd | Separating method for carbon monoxide gas |
| JPS5339289A (en) * | 1976-09-22 | 1978-04-11 | Hitachi Ltd | Separating method for carbon monoxide |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5610681A (en) | 1981-02-03 |
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