JPH01304184A - Manufacture of methane-containing gas - Google Patents
Manufacture of methane-containing gasInfo
- Publication number
- JPH01304184A JPH01304184A JP13432488A JP13432488A JPH01304184A JP H01304184 A JPH01304184 A JP H01304184A JP 13432488 A JP13432488 A JP 13432488A JP 13432488 A JP13432488 A JP 13432488A JP H01304184 A JPH01304184 A JP H01304184A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- alcohol
- carbon dioxide
- pipe
- reaction product
- 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
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 27
- 238000004519 manufacturing process Methods 0.000 title claims description 11
- 238000010521 absorption reaction Methods 0.000 claims abstract description 52
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 29
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 25
- 238000000926 separation method Methods 0.000 claims abstract description 14
- 239000007791 liquid phase Substances 0.000 claims abstract description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 104
- 239000007789 gas Substances 0.000 claims description 60
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 52
- 239000001569 carbon dioxide Substances 0.000 claims description 51
- 239000007788 liquid Substances 0.000 claims description 39
- 229930195733 hydrocarbon Natural products 0.000 claims description 11
- 150000002430 hydrocarbons Chemical class 0.000 claims description 11
- 239000002994 raw material Substances 0.000 claims description 11
- 239000011261 inert gas Substances 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 238000000034 method Methods 0.000 abstract description 24
- 238000006243 chemical reaction Methods 0.000 abstract description 9
- 238000009792 diffusion process Methods 0.000 abstract description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 42
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 10
- 150000001412 amines Chemical class 0.000 description 6
- 238000001816 cooling Methods 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 5
- 230000008929 regeneration Effects 0.000 description 5
- 238000011069 regeneration method Methods 0.000 description 5
- 229910000027 potassium carbonate Inorganic materials 0.000 description 4
- 235000011181 potassium carbonates Nutrition 0.000 description 4
- 239000007864 aqueous solution Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- MYTMXVHNEWBFAL-UHFFFAOYSA-L dipotassium;carbonate;hydrate Chemical compound O.[K+].[K+].[O-]C([O-])=O MYTMXVHNEWBFAL-UHFFFAOYSA-L 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229940072033 potash Drugs 0.000 description 2
- 235000015320 potassium carbonate Nutrition 0.000 description 2
- 239000003507 refrigerant Substances 0.000 description 2
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 1
- -1 amine compounds Chemical class 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、新規な炭酸ガス除去法を使用したアルコール
からのメタン含有ガス（以下、ＳＮＧと記す）の製造法
である。アルコールよりのＳ Ｎ Ｇ Ｗ進法は、安価
で輸送および貯蔵に容易なアルコールを原料とし、より
簡便にＳＮＧが得られる方法として都市ガス製造法等に
おいて最近注目されている。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention is a method for producing methane-containing gas (hereinafter referred to as SNG) from alcohol using a novel carbon dioxide removal method. The S N G W base method from alcohol has recently been attracting attention in city gas production methods, etc. as a method for obtaining SNG more easily using alcohol, which is inexpensive and easy to transport and store, as a raw material.
アルコールからのメタン含有ガスの製造法は、例えば特
開昭５３−３５７０２号および特開昭５３−１０１３０
５号などから公知であり、この製造工程はアルコールと
水ア気とを反応させてメタンなどを含む反応生成ガスを
製造する反応工程と、反応生成ガス中の不要成分である
ＣＯ□などを除去する炭酸ガス分離工程からなっている
。Methods for producing methane-containing gas from alcohol are described, for example, in JP-A-53-35702 and JP-A-53-10130.
No. 5, etc., and this production process involves a reaction process in which alcohol and water atom are reacted to produce a reaction product gas containing methane, and unnecessary components such as CO□ in the reaction product gas are removed. The process consists of a carbon dioxide gas separation process.
炭酸ガス分離工程においては、ＣＯ□吸収液として加熱
された炭酸カリウム水）８液（熱炭酸カリ法）や、モノ
エタノールアミンやジェタノールアミン等のアミン系化
合物を主体とする水溶液（アミン法）が用いられ、加熱
による吸収液の再生を行うのが−船釣である。In the carbon dioxide gas separation process, 8 liquids of heated potassium carbonate water (heated potassium carbonate water) as the CO□ absorption liquid (heated potassium carbonate method) and an aqueous solution mainly containing amine compounds such as monoethanolamine and jetanolamine (amine method) are used. In boat fishing, the absorption liquid is regenerated by heating.
従来の熱炭酸カリ法やアミン法においては、炭酸ガス分
離工程での吸収液の再生に多量の熱が必要であり、この
所要熱量が反応工程で得られる熱量よりも大きくなるの
で、ＳＮＧ装置全体としての熱量が不足となり、ボイラ
設備等が更に必要である。In the conventional hot potash carbonate method and amine method, a large amount of heat is required to regenerate the absorption liquid in the carbon dioxide gas separation process, and this required amount of heat is larger than the amount of heat obtained in the reaction process, so the entire SNG equipment As a result, additional boiler equipment is required.
また吸収液である熱炭酸カリやアミン水溶液の貯蔵設備
を別途必要とし、起動および停止などの操作性が難しい
という欠点がある。更にこれらの吸収液は通常腐食性が
激しいため、炭酸ガス分離工程の吸収塔、再生塔および
配管などには耐食性材料を用いるか、或は吸収液中に防
食材を添加するなどの対策が必要であった。Another disadvantage is that it requires separate storage equipment for the absorption liquid, such as hot potassium carbonate or amine aqueous solution, and is difficult to operate, such as starting and stopping. Furthermore, these absorption liquids are usually highly corrosive, so it is necessary to take measures such as using corrosion-resistant materials for the absorption tower, regeneration tower, piping, etc. in the carbon dioxide separation process, or adding anti-corrosive substances to the absorption liquid. Met.
熱炭酸カリ法においては、アミン法に比べて吸収液の再
生には多く・の熱源を必要としないが、高温の熱源を必
要とし、またプラント停止時には吸収液の温度が低下し
て固結するのを避けるため常に熱を加えて循環しておく
必要があるなどの欠点がある。The hot potash carbonate method does not require as many heat sources to regenerate the absorbent compared to the amine method, but it does require a high-temperature heat source, and when the plant is shut down, the temperature of the absorbent drops and solidifies. It has disadvantages such as the need to constantly apply heat and circulate it to avoid this.
発明者等は、上記の如き問題点を有するＳＮＧ装置につ
いて鋭意検討した結果、炭酸ガス分離工程に用いる吸収
液に熱炭酸カリやアミン水溶液に代えて、原料である液
相アルコールを用いること等により問題点が解決される
ことを見出し、本発明に至った。As a result of intensive study on SNG devices having the above-mentioned problems, the inventors discovered that the solution was to use liquid-phase alcohol as a raw material instead of hot potassium carbonate or amine aqueous solution as the absorption liquid used in the carbon dioxide gas separation process. The inventors have discovered that the problem can be solved, and have arrived at the present invention.
即ち本発明は、
（１）アルコールと水蒸気とを反応させ、反応生成ガス
中の炭酸ガスを分離する工程を有するメタン含有ガスの
製造法において、炭酸ガス分離工程における吸収液に原
料の液相アルコールを用いることを特徴とするメタン含
有ガスの製造法、（２）反応生成ガス中の炭酸ガスおよ
び炭化水素の一部を吸収した吸収液を炭酸ガス放散塔へ
の供給前に減圧し、分離された炭酸ガスおよび炭化水素
を反応生成ガスと共に炭酸ガス吸収塔に導く方法、（３
）炭酸ガス放散塔において空気または不活性ガスを用い
る方法である。That is, the present invention provides: (1) In a method for producing a methane-containing gas, which includes a step of reacting alcohol and water vapor and separating carbon dioxide from the reaction product gas, liquid-phase alcohol as a raw material is added to the absorption liquid in the carbon dioxide gas separation step. A method for producing a methane-containing gas characterized by using (2) an absorption liquid that has absorbed part of carbon dioxide and hydrocarbons in the reaction product gas, which is depressurized before being supplied to a carbon dioxide stripping tower, and separated. A method for introducing carbon dioxide and hydrocarbons together with reaction product gas into a carbon dioxide absorption tower, (3)
) This is a method using air or inert gas in a carbon dioxide gas stripping tower.
本発明における反応工程では、通常ニッケル系触媒を使
用し、メタノールを主成分とする混合アルコールと水蒸
気とを、反応温度２００〜５００ ’Ｃ１圧力５〜５０
ｋｇ／ｃｍ”Ｇで反応させる。In the reaction step of the present invention, a nickel-based catalyst is usually used, and a mixed alcohol containing methanol as a main component and water vapor are heated at a reaction temperature of 200 to 500'C1 pressure of 5 to 50%.
React at kg/cm”G.
本発明の炭酸ガス分離工程においては、原料のアルコー
ル液を吸収液に用いるので、できるだけ低温で吸収を行
うことが望ましく、原料液の蒸発および加熱、水蒸気回
収等により反応生成ガスの熱回収を行い、更に冷媒で冷
却して反応生成ガス中の水分を凝縮分離した後、炭酸ガ
ス吸収塔に供給する。In the carbon dioxide separation process of the present invention, since the raw alcohol liquid is used as the absorption liquid, it is desirable to perform the absorption at as low a temperature as possible, and the heat of the reaction product gas is recovered by evaporation and heating of the raw material liquid, steam recovery, etc. The reaction product gas is further cooled with a refrigerant to condense and separate moisture in the reaction product gas, and then supplied to a carbon dioxide absorption tower.
吸収塔の温度は、−５０〜０°Ｃ２好ましくは−３０〜
−１０°Ｃである。吸収塔の温度がＯ″Ｃより高い場合
には、吸収液の循環量を多くする必要があり、また吸収
塔および再生塔から排出されるガス中に同伴されるアル
コールの量が増大するので、その１員失量が多くなる。The temperature of the absorption tower is -50 to 0°C2, preferably -30 to
-10°C. When the temperature of the absorption tower is higher than O''C, it is necessary to increase the circulation amount of the absorption liquid, and the amount of alcohol entrained in the gas discharged from the absorption tower and the regeneration tower increases. The loss of that one member will increase.
吸収塔の温度を一５０°Ｃより低い場合には冷媒の負荷
の点より経済的でない。If the temperature of the absorption tower is lower than -50°C, it is not economical due to the load on the refrigerant.
本発明での炭酸ガス吸収塔の圧力は反応条件により左右
され、通常２〜５０ｋｇ／ｃｍ”Ｇ 、好ましくは５〜
２０ｋｇ／ｃｍ２Ｇである。吸収塔の圧力が低過ぎる場
合には、アルコール液でのＣＯ２吸収量が減少するため
、吸収液の循環量を多くする必要があり、吸収塔径およ
び循環動力が大きくなる。吸収塔の圧力が高過ぎる場合
には吸収塔の肉厚が大きくなり、また吸収液への炭化水
素の溶解量が増えるので損失量が多くなり原料原単位が
悪化する。The pressure of the carbon dioxide absorption tower in the present invention depends on the reaction conditions, and is usually 2 to 50 kg/cm"G, preferably 5 to 50 kg/cm"G.
It is 20kg/cm2G. If the pressure of the absorption tower is too low, the amount of CO2 absorbed by the alcohol liquid decreases, so it is necessary to increase the amount of circulation of the absorption liquid, which increases the diameter of the absorption tower and the circulation power. If the pressure of the absorption tower is too high, the wall thickness of the absorption tower will increase, and the amount of hydrocarbons dissolved in the absorption liquid will increase, resulting in an increased amount of loss and a worsening of the raw material consumption rate.
（２）の発明で、反応生成ガス中の炭酸ガスおよび炭化
水素の一部を吸収した吸収液を炭酸ガス再生塔への供給
前に減圧し、分離された炭酸ガスおよび炭化水素を反応
生成ガスと共に炭酸ガス吸収塔に導くことにより、上記
の炭化水素の損失量が減少し、原料原単位が改善される
。なお減圧時の圧力は、放散塔が常圧付近で通常運転さ
れることから０．５〜５ｋｇ／ｃｍ２Ｇ程度とする。In the invention of (2), the absorption liquid that has absorbed part of the carbon dioxide and hydrocarbons in the reaction product gas is depressurized before being supplied to the carbon dioxide regeneration tower, and the separated carbon dioxide and hydrocarbons are converted into the reaction product gas. By introducing the carbon dioxide into the carbon dioxide absorption tower, the amount of loss of the hydrocarbons described above is reduced, and the raw material consumption rate is improved. Note that the pressure during depressurization is approximately 0.5 to 5 kg/cm2G since the stripping tower is normally operated near normal pressure.
本発明の方法における吸収液の再生操作は、反応工程で
回収される水蒸気等により加熱して行うこともできるが
、加熱による再生の場合には吸収塔への循環液の冷却負
荷が大きくなり、低温の冷却源が大量に必要となる。こ
れに対しては、（３）の発明により空気または不活性ガ
スを放散塔に導入することが有効である。放散塔は通常
は常圧付近で操作されるが、減圧下で操作してもよい。The regeneration operation of the absorption liquid in the method of the present invention can also be carried out by heating with water vapor etc. recovered in the reaction step, but in the case of regeneration by heating, the cooling load of the circulating liquid to the absorption tower becomes large. Large quantities of low-temperature cooling sources are required. For this purpose, it is effective to introduce air or an inert gas into the stripping tower according to the invention (3). The stripping tower is usually operated near normal pressure, but may also be operated under reduced pressure.
この場合には空気または不活性ガスの導入量を減らすこ
とができる。不活性ガスとしては窒素や工場より排出さ
れる不活性ガスをを効に利用することができる。In this case, the amount of air or inert gas introduced can be reduced. As the inert gas, nitrogen or an inert gas discharged from a factory can be effectively used.
次に本発明の理解を容易とするために、反応生成ガスか
らの炭酸ガス分離工程に於ける吸収液として原料である
液相アルコールを用いるメタン含有ガスの製造法のフロ
ーの例を添付の図面を用いて説明する。Next, in order to facilitate understanding of the present invention, an example of the flow of a method for producing methane-containing gas using liquid phase alcohol, which is a raw material, as an absorption liquid in the process of separating carbon dioxide gas from reaction product gas is shown in the accompanying drawings. Explain using.
第１図は、本発明のプロセスの一例を示すフローであり
、いずれのプロセスも原料アルコールとしてメタノール
を用いる場合である。FIG. 1 is a flowchart showing an example of the process of the present invention, in which methanol is used as the raw material alcohol in each process.
第１図において、反応生成ガスは原料アルコールの予熱
或はガス化など熱回収により冷却後、更に冷却され、反
応生成ガス中の水分が除去され、管１より炭酸ガス分離
工程導入される。吸収液はフラッシュタンク〔Ｆ〕にお
いて減圧されて炭化水素等の溶解ガスが分離され、その
ガスは管５を経てＮ環機（Ｋ）に導入され昇圧され、管
６を経て前記管ｌからの反応生成ガスと合流し、管２を
経て炭酸ガス吸収塔（Ｔ）に導入される。In FIG. 1, the reaction product gas is cooled by heat recovery such as preheating or gasification of the raw material alcohol, and then further cooled to remove water in the reaction product gas, and then introduced through a pipe 1 into a carbon dioxide gas separation process. The absorption liquid is depressurized in the flash tank [F] to separate dissolved gases such as hydrocarbons, and the gas is introduced into the N-ring machine (K) through pipe 5, where the pressure is increased, and then through pipe 6 from the pipe 1. It joins with the reaction product gas and is introduced into the carbon dioxide absorption tower (T) via pipe 2.
炭酸ガス吸収塔では、上段から補給用のメタノールが管
１４より導入され、中段からは循環メタノール液が管１
３より導入される。一方吸収塔塔頂からは、反応生成ガ
ス中の炭酸ガスが除去されたＳＮＧが管３から得られる
。また吸収塔塔底からは反応生成ガス中の炭酸ガスを吸
収した循環メタノール吸収液が管４を通してフランシュ
タンクに導入される。In the carbon dioxide absorption tower, methanol for replenishment is introduced from the upper stage through pipe 14, and circulating methanol liquid is introduced from the middle stage through pipe 1.
It will be introduced from 3. On the other hand, from the top of the absorption tower, SNG from which carbon dioxide gas in the reaction product gas has been removed is obtained from a pipe 3. Further, from the bottom of the absorption tower, a circulating methanol absorption liquid that has absorbed carbon dioxide gas in the reaction product gas is introduced into the Franche tank through a pipe 4.
炭酸ガス放散塔ＣＤ）においては、フランシュタンクで
分離された液が管７より上段に導かれ、空気がブロア（
Ｂ）により管８を通して下段に導入される。放散塔塔頂
からは吸収液中の炭酸ガス、微量の炭化水素および空気
がオフガスとして管９より糸外に排出される。また放散
塔塔底からは、再生メタノール液が管１０より排出され
、その一部が反応装置に供給される原料メタノールとし
て管１１より送られ、残部は管１２、循環メタノール吸
収液冷却器〔Ｅ〕、管１３を通して炭酸ガス吸収塔に戻
され循環使用される。In the carbon dioxide gas stripping tower CD), the liquid separated in the Franche tank is led to the upper stage from the pipe 7, and air is passed through the blower (CD).
B) is introduced into the lower stage through tube 8. From the top of the stripping column, carbon dioxide, trace amounts of hydrocarbons, and air in the absorption liquid are discharged as off-gas through the tube 9 to the outside. Also, from the bottom of the stripping tower, regenerated methanol liquid is discharged from pipe 10, a part of which is sent from pipe 11 as raw methanol to be supplied to the reaction apparatus, and the remainder is sent from pipe 12 to circulating methanol absorption liquid cooler [E ], is returned to the carbon dioxide absorption tower through the pipe 13 and used for circulation.
なお本発明は上記のフローを図面により限定されるもの
ではなく、例えば炭酸ガスの放散効果をより大きくする
ため放散塔塔底液を加熱することや、管９に真空ポンプ
を設は放散塔の圧力を真空とすることなど、種々の変更
を加えることができる。Note that the present invention is not limited to the flow described above by the drawings, and for example, heating the bottom liquid of the stripping tower in order to increase the carbon dioxide diffusion effect, or installing a vacuum pump in the pipe 9, etc. Various changes can be made, such as changing the pressure to a vacuum.
次に本発明の炭酸ガス分離プロセスについての検討例を
示し、効果を具体的に説明する。Next, a study example of the carbon dioxide gas separation process of the present invention will be shown, and the effects will be specifically explained.
１、条件
炭酸ガス分離プロセスとして添付の第１図のフローに基
づいて検討した。主な条件は下記の通りである。1. Conditions The carbon dioxide gas separation process was studied based on the flow shown in the attached Figure 1. The main conditions are as follows.
（１）反応生成ガス〔管ｌ〕
流ｆｆｉ Ｃ８４７，５ｋｇｍｏｌ／ｈＣ０２２，５
ｋｇｍｏｌ／ｈ
（２）炭酸ガス吸収塔〔Ｔ〕
圧力 ８．７ ａｔｍ
温 度 塔頂 −２０°Ｃ
塔底 −１５°Ｃ
（３）フラッシュタンクＣＦ）
圧力 ２．Ｏａｔｍ
温度 −１５°Ｃ
（４）炭酸ガス放散塔ＣＤ’１
圧力 １．０ ａｔｍ
温度 −１５°Ｃ
（５）循環メタノール吸収液〔管１２〕流ｉｔ
９８．７ ｋｇｍｏｌ／ｈ（６）補給メタノール〔管
１４〕
流”１ １０．０ ｋｇｍｏｌ／ｈ（７）炭酸ガ
ス放散塔への空気〔管８］流”Ｉｆ ３．７
Ｊｍｏｌ／ｈ■、結果
（１）ＳＮＧ［管３］
ｉ １ ＣＨ４７，４１ｋｇｍｏｌ／ｈＣ○２
０．３０ ｋｇｍｏｌ／ｈ（２）フランシュタンク
での放散ガス〔管５〕流ｆｆｌ ＣＨ４０，３５ｋｇ
ｍｏｌ／ｈＣ０２０，５６ｋｇｍｏｌ／ｈ
（３）炭酸ガス放散塔からのオフガス〔管９〕流量 Ｃ
Ｈ４０，０９ｋｇｍｏｌ／ｈ
ＣＯ２２，１１ｋｇｍｏｌ／ｈ
空気 ３．７ ｋｇｍｏｌ／ｈ（４）原料メタ
ノール〔管１１〕
流 量 メタノール １０．Ｏｋ
ｇｍｏｌ／ｈＣ０２０，０９ｋｇｍｏｌ／ｈ
（５）炭酸ガスの除去率 ８８ ％（６）Ｓ
ＮＧ中の ＣＨ４回収率 ９９ ％（７）循環メタ
ノール吸収液冷却器（Ｅ）冷却熱Ｗｋ
８．７ Ｍｃａｌ／ｈ（８）回転機械の所要動力
３ ｋｗ〔発明の効果〕
本発明の方法によれば、実施例に示される如く非常に少
ない熱負荷（冷却負荷）で効率よ（反応生成ガス中の炭
酸ガスを除去することができる。(1) Reaction product gas [tube 1] Flow ffi C847,5 kgmol/hC022,5
kgmol/h (2) Carbon dioxide absorption tower [T] Pressure 8.7 atm Temperature Tower top -20°C Tower bottom -15°C (3) Flash tank CF) Pressure 2. Oatm temperature -15°C (4) Carbon dioxide gas stripping tower CD'1 pressure 1.0 atm temperature -15°C (5) Circulating methanol absorption liquid [tube 12] flow it
98.7 kgmol/h (6) Make-up methanol [tube 14] Flow 1 10.0 kgmol/h (7) Air to carbon dioxide gas stripping tower [tube 8] Flow If 3.7
Jmol/h■, result (1) SNG [tube 3] i 1 CH47, 41kgmol/hC○2
0.30 kgmol/h (2) Diffusion gas [tube 5] flow in Franche tank ffl CH40, 35kg
mol/hC020, 56 kgmol/h (3) Flow rate of off gas from the carbon dioxide gas stripping tower [pipe 9] C
H40, 09 kgmol/h CO22, 11 kgmol/h Air 3.7 kgmol/h (4) Raw material methanol [tube 11] Flow rate Methanol 10. Ok
gmol/hC020,09kgmol/h (5) Carbon dioxide removal rate 88% (6) S
CH4 recovery rate in NG 99% (7) Circulating methanol absorption liquid cooler (E) Cooling heat Wk
8.7 Mcal/h (8) Required power of rotating machinery
3 kW [Effects of the Invention] According to the method of the present invention, carbon dioxide gas in the reaction product gas can be efficiently removed with a very small heat load (cooling load) as shown in the examples.
即ち上記実施例における冷却熱量は単位ＣＯ□当り１８
４ｋｃａｌ／Ｎｍ”であり、これは従来の熱炭酸カリ法
の場合（約１５００ｋｃａ ｌ／Ｎｍ３）やアミン法の
場合（約２５００ｋｃａ ｌ／Ｎｍリ と比較しても非
常に少なく、冷却負荷となることを考慮しても有利であ
る。That is, the amount of cooling heat in the above example is 18 per unit CO□.
4kcal/Nm", which is very small compared to the conventional hot potassium carbonate method (approximately 1500kcal/Nm3) or the amine method (approximately 2500kcal/Nm3), and does not result in a cooling load. It is advantageous to take this into account.
更に本発明の方法・は次のような特徴を有し、アルコー
ルよりのＳＮＧ製造装置において極めて優れた方法であ
る。Furthermore, the method of the present invention has the following characteristics and is an extremely excellent method in an apparatus for producing SNG from alcohol.
（１）炭酸ガスの吸収液に原料アルコールを用いるので
、吸収液のための別個の貯蔵設備等が不要であり、設備
費が削減されると共に、起動、停止操作が容易である。(1) Since raw alcohol is used as the carbon dioxide absorption liquid, there is no need for separate storage equipment for the absorption liquid, equipment costs are reduced, and startup and shutdown operations are easy.
（２）吸収液の腐蝕性が低いので、耐蝕性材料が不要で
あり、また吸収液の劣化や固結も起こらないので、この
点よりも設備費および運転操作上有利である。(2) Since the absorbing liquid is less corrosive, no corrosion-resistant material is required, and the absorbing liquid does not deteriorate or solidify, which is more advantageous in terms of equipment costs and operation.
（３）吸収液を放散塔の前で減圧し、フラッシュタンク
で溶解ガスを回収することにより、炭化水素の損失量が
削減され、原料アルコールの原単位が向上する。(3) By reducing the pressure of the absorption liquid in front of the stripping tower and recovering the dissolved gas in the flash tank, the loss of hydrocarbons is reduced and the basic unit of raw alcohol is improved.
（４）炭酸ガス放散塔に空気または不活性ガスを用いる
ことにより、炭酸ガス分離工程における消費エネルギー
が削減され、また運転操作も容易である。(4) By using air or an inert gas for the carbon dioxide gas stripping tower, the energy consumption in the carbon dioxide separation process is reduced and the operation is easy.
第１図は本発明の炭酸ガス分離プロセスの工程図の例で
あり、各略号は以下の通りである。
Ｔ：炭酸ガス吸収塔、Ｆ：フラッシュタンク、Ｄ：炭酸
ガス放散塔、Ｋ：循環機、ＢニブロアＥ：循環メタノー
ル吸収液冷却器FIG. 1 is an example of a process diagram of the carbon dioxide gas separation process of the present invention, and each abbreviation is as follows. T: Carbon dioxide absorption tower, F: Flash tank, D: Carbon dioxide diffusion tower, K: Circulator, B Niblower E: Circulating methanol absorption liquid cooler
Claims (3)
中の炭酸ガスを分離する工程を有するメタン含有ガスの
製造法において、炭酸ガス分離工程における吸収液に原
料の液相アルコールを用いることを特徴とするメタン含
有ガスの製造法。(1) A method for producing methane-containing gas that includes a step of reacting alcohol and water vapor and separating carbon dioxide from the reaction product gas, characterized in that liquid-phase alcohol as a raw material is used as an absorption liquid in the carbon dioxide gas separation step. A method for producing methane-containing gas.
を吸収した吸収液を炭酸ガス放散塔への供給前に減圧し
、分離された炭酸ガスおよび炭化水素を反応生成ガスと
共に炭酸ガス吸収塔に導く請求項１記載のメタン含有ガ
スの製造法。(2) The absorption liquid that has absorbed part of the carbon dioxide and hydrocarbons in the reaction product gas is depressurized before being supplied to the carbon dioxide stripping tower, and the separated carbon dioxide and hydrocarbons are absorbed together with the reaction product gas. The method for producing methane-containing gas according to claim 1, wherein the methane-containing gas is introduced into a column.
用いる請求項１または２記載のメタン含有ガスの製造法(3) The method for producing methane-containing gas according to claim 1 or 2, wherein air or an inert gas is used in the carbon dioxide gas stripping tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13432488A JPH01304184A (en) | 1988-06-02 | 1988-06-02 | Manufacture of methane-containing gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13432488A JPH01304184A (en) | 1988-06-02 | 1988-06-02 | Manufacture of methane-containing gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH01304184A true JPH01304184A (en) | 1989-12-07 |
Family
ID=15125657
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP13432488A Pending JPH01304184A (en) | 1988-06-02 | 1988-06-02 | Manufacture of methane-containing gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH01304184A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH1045679A (en) * | 1996-04-17 | 1998-02-17 | Jgc Corp | Production of carbonic acid diester, removal of carbon dioxide, carbon dioxide absorbent and apparatus for producing carbonic acid diester |
-
1988
- 1988-06-02 JP JP13432488A patent/JPH01304184A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH1045679A (en) * | 1996-04-17 | 1998-02-17 | Jgc Corp | Production of carbonic acid diester, removal of carbon dioxide, carbon dioxide absorbent and apparatus for producing carbonic acid diester |
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