JPS6118732A - Concentration of isobutylene in c4 hydrocarbons - Google Patents

Concentration of isobutylene in c4 hydrocarbons

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Publication number
JPS6118732A
JPS6118732A JP59140383A JP14038384A JPS6118732A JP S6118732 A JPS6118732 A JP S6118732A JP 59140383 A JP59140383 A JP 59140383A JP 14038384 A JP14038384 A JP 14038384A JP S6118732 A JPS6118732 A JP S6118732A
Authority
JP
Japan
Prior art keywords
butene
hydrogen
isomerization
hydroisomerization
hydrogenative
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
Application number
JP59140383A
Other languages
Japanese (ja)
Inventor
Ichiro Imai
今井　市郎
Atsushi Matsuura
淳 松浦
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Mitsui Petrochemical Industries Ltd
Original Assignee
Mitsui Petrochemical Industries Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Mitsui Petrochemical Industries Ltd filed Critical Mitsui Petrochemical Industries Ltd
Priority to JP59140383A priority Critical patent/JPS6118732A/en
Publication of JPS6118732A publication Critical patent/JPS6118732A/en
Pending legal-status Critical Current

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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
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Abstract

PURPOSE:Butene-1 in C4 hydrocarbon fraction is converted into butene-2 under specific hydrogenative isomerization conditions to facilitate fractional distillation whereby isobutylene used as a starting material for t-butanol is obtained in high yield. CONSTITUTION:In the concentration of isobutylele by hydrogenative isomerization of butene-1 into butene-2 in C4 hydrocarbon fraction, the hydrogenative isomerization is carried out by feeding hydrogen in such an amount as the equation is satisfied (Y is the amount of hydrogen in moles; X is conversion of butene-1 in %; Z is the total mole number of dienes and acetylenes in the hydrocarbon fraction). Then, the reaction mixture is subjected to distillation to separate of the lower and high-boiling fractions. The process is preferably operated in the order of ow-boiling cut, hydrogenative isomerization and high boiling cut. Further, it is preferred that a plurality of reactors are used in series to effect hydrogenative isomerization, as hydrogen is fed to each reactor.

Description

【発明の詳細な説明】 発明の目的 ［産業上の利用分野］ 本発明は、Ｃ４炭化水素混合物中に含有されているイソ
ブチレンの濃縮方法に関する。　ｉｑられたイソブチレ
ン濃縮混合物は、ｔｅｒｔ−ブタノール（以下ｒＴＢ△
」と略称づることがある）の合成、２．６−シーｔａｒ
ｔ−ブヂルフ〕−ノール（以下「２゜６−　Ｄ　Ｔ　［
３Ｐ　Ｊと略称づることがある）あるいはアルキル化剤
等の原料どして使われる。DETAILED DESCRIPTION OF THE INVENTION OBJECTS OF THE INVENTION [Industrial Field of Application] The present invention relates to a method for concentrating isobutylene contained in a C4 hydrocarbon mixture. The iq isobutylene concentrated mixture is tert-butanol (hereinafter referred to as rTB△
), the synthesis of 2.6-sheet tar
t-builf]-nol (hereinafter referred to as “2゜6-D T [
It is sometimes abbreviated as 3PJ) or used as a raw material for alkylating agents, etc.

［従来の技術］ Ａレフインブラン１〜で得られるＣ４炭化水素混合物、
いわゆるＢＢ留分け、まずその中のブタジェンをどり出
し、残ったＳＢＢ留分中の有用な成分であるイソブチレ
ンを、抽出、吸着まｌζは蒸留等により濃縮して利用覆
る。　ところが、ＳＢＢ留分中のイソブチレンとブテン
−１とは、沸点が近接していて（前者は−６，９°ｃ、
′ｆ：を当は−６゜３°Ｃ）、蒸留（こよる分離（よ困
難である。[Prior art] C4 hydrocarbon mixture obtained from A Refin Blanc 1~,
In the so-called BB distillation, first the butadiene in it is extracted, and isobutylene, which is a useful component in the remaining SBB fraction, is extracted and adsorbed, and the remaining SBB fraction is concentrated and utilized by distillation. However, isobutylene and butene-1 in the SBB fraction have close boiling points (the former has a boiling point of -6.9°C,
'f: is -6°3°C), distillation (and separation (more difficult).

一方、ブテン−２は、沸点がシス型３．７℃、１ヘラン
ス望０．９°Ｃとブテン−１よりも商くなるので、イソ
ブチンと蒸留により分１１１１−９−ることかできる。On the other hand, butene-2 has a boiling point of 3.7° C. in the cis form and 0.9° C. in the cis form, which is lower than that of butene-1, so it can be separated by distillation with isobutene.

　従って、Ｃ４炭化水素混合物中のブテン−１をブテン
−２（ご転化させれば、イソブチレンのｉお縮かできる
。。Therefore, by converting butene-1 in a C4 hydrocarbon mixture to butene-2, isobutylene can be reduced.

【発明か解決しようとする問題点１ 本発明の目的は、Ｃ／１炭化水系中のイソブチレンを利
用づるために濃縮づるにあ／ζす、水素添加に」、る異
性化反応（以下１−水添界１／４化」と略称することが
ある）によりブテン−１をブテン−２に転化さゼで蒸留
分離を容易に覆る工程を含む方法を、最も効果的に実施
する条例を確立することにある。Problem to be Solved by the Invention 1 The object of the present invention is to solve the isomerization reaction (hereinafter 1- Establish regulations to most effectively implement a process that involves the conversion of 1-butene to 2-butene by hydrogenation (sometimes abbreviated as "hydrogenation 1/4"), which easily overrides the distillation separation. There is a particular thing.

発明の構成 【問題を解決するための手段］ 本発明のＣ４炭化水累中のイソブチレンを濃縮する方法
は、Ｃ４炭化水素を水添異性化触媒を充填した反応器に
水素を添加しながら供給１．てＣ４炭化水素中のブテン
−１をブテン−２に異性化する水添異性化工程、低沸分
を除去ターる蒸留分離工程および高８１ｊ分を除去する
蒸留分囚１工程からなり、」：記の水添層性化工程を、 Ｙ≧Ｚ　（Ｘ＋４．１４）／４．４２３Ｘ０．５Ｙ：水
素は（モル数） ×ニブテンー１の転化率（％） Ｚ：０４炭化水素中のジエン類およびアセチレン類の総
モル数 の関係式を満足する（ｄの水素の添加の下に実施するこ
とを特徴とする。Structure of the Invention [Means for Solving the Problem] The method for concentrating isobutylene in a C4 hydrocarbon accumulation of the present invention comprises supplying C4 hydrocarbons to a reactor filled with a hydroisomerization catalyst while adding hydrogen. ．． It consists of a hydroisomerization step in which butene-1 in C4 hydrocarbons is isomerized to butene-2, a distillation separation step to remove low-boiling components, and a distillation fractionation step to remove high-boiling components. The hydrogenation stratification step is as follows: Y≧Z (X+4.14)/4.423X0.5Y: Hydrogen is (number of moles) × conversion rate of nibten-1 (%) It satisfies the relational expression of the total number of moles of acetylenes (characterized in that it is carried out under the addition of hydrogen in d).

【作用］ 上記の条件をみたす十分な量の水素を添加しつつ、Ｃ４
炭化水素中に含有されＣいるブテン−１をブテン−２に
水添異性化することにより、異性化の転化率が高くなり
、高回収率でイソブチレンを得ることができる。[Operation] While adding sufficient amount of hydrogen to satisfy the above conditions, C4
By hydroisomerizing butene-1 contained in hydrocarbons to butene-2, the conversion rate of isomerization increases and isobutylene can be obtained with a high recovery rate.

（実施態様） 低沸分を除去する蒸留分画ＩＪ−程、水添異性化工程お
よび高沸分を除去する蒸留分離工程の３工程を実７ＩＩ
！ｉする順序は任意であり、イソブチレンの濃縮率はそ
れにＪ、って実質上具なることはない。(Embodiment) The three steps of distillation fraction IJ-process for removing low-boiling components, hydroisomerization step, and distillation separation step for removing high-boiling components are carried out in 7II.
! The order of i is arbitrary, and the concentration ratio of isobutylene is substantially independent of J.

しかし、最初に低沸分を除去した上−Ｃ水添異性化を行
ない、その後に高１ｄｌｉ分を除去づることが好ましい
。　低沸分の除去により、Ｃ，１炭化水素中に含有され
ているプロパジエンおよびメヂルアセヂレンなどがまり
“除去され、異↑（（化Ｔ稈における水素のン肖費叩が
節減で゛ぎるからである。However, it is preferable to first perform the upper-C hydrogenation isomerization by removing the low-boiling fraction, and then to remove the high-boiling fraction. By removing low-boiling components, propadiene and methyl acetylene contained in C,1 hydrocarbons are removed, resulting in a difference ↑ ((This is because the cost of hydrogen in the chemical T culm is too reduced. .

原料であるＣ４炭化水素中の水分および一酸化炭素は、
蒸留等の方法Ｃあらかじめ除去しておく。Moisture and carbon monoxide in the raw material C4 hydrocarbon are
Method C such as distillation etc. Remove in advance.

しかし、この操作は、水添異性化反応器稈の前に行なえ
ばよい。However, this operation may be performed before the hydroisomerization reactor culm.

水添異性化反応器に充填する触媒は、常用のものからえ
らべばよいが、゛不活性アルミナを単体として、パラジ
ウムを０．１〜３．０重量％担持さゼた触媒が好適であ
る。　供給するＣ４炭化水素の流量は、触媒の充填量に
対して０．０５−１０く容量比）／ｈｒとづる。　好ま
しくは０．０７〜２（容量比）、／ｈｒである。The catalyst to be filled in the hydrogen isomerization reactor may be selected from commonly used catalysts, but a catalyst containing 0.1 to 3.0% by weight of palladium supported on inert alumina is preferred. The flow rate of C4 hydrocarbon to be supplied is expressed as 0.05-10 (capacity ratio)/hr with respect to the filling amount of the catalyst. Preferably it is 0.07 to 2 (capacity ratio)/hr.

水添異性化反応器に供給する水素の辺は、前記しｌ〔 Ｙ≧７（Ｘ＋４．１　／４　）／４．１！１２．３ｘＯ
，５の関係式をみたす量であるが、好ましい和は、Ｙ≧
Ｚ　（Ｘ＋４．、１４．）　／４．４２３の式を満足η
る吊（ある。　なｄ５、あまりに水素の借が過剰ひある
と、触媒の利用効果が低下し、運転動力が増大し、しか
もイソブチレンへの好ましくない水添が起ることもある
から、水素過剰率としでは３０００％イ」近を−Ｌ限と
考えるべきである。The side of hydrogen supplied to the hydroisomerization reactor is as shown above: [Y≧7(X+4.1/4)/4.1!12.3xO
, 5, but the preferable sum is Y≧
Satisfies the formula Z (X+4., 14.) /4.423 η
(d5) If there is too much hydrogen, the effectiveness of the catalyst will decrease, the operating power will increase, and undesirable hydrogenation to isobutylene may occur. In terms of rate, the -L limit should be considered to be close to 3000%.

反応条件は、系が液相を保つよう、温度は０〜１００℃
、りｆましくは、１０〜５０°Ｃ１、圧力は５〜５０Ｋ
（＋　／ｃｍ２　Ｇ、好ましくは７〜３０Ｋｇ／ｃｍ２
Ｑの範囲からえらふ。The reaction conditions were a temperature of 0 to 100°C to maintain the liquid phase of the system.
, preferably 10~50°C1, pressure 5~50K
(+/cm2 G, preferably 7-30Kg/cm2
Choose from the range of Q.

水添異性化反応器は、複数段を直列に接続し、各反応器
に供給する水素の量か十記条件式を満足するようにする
ことが好ましい、。It is preferable that the hydrogen isomerization reactor has a plurality of stages connected in series so that the amount of hydrogen supplied to each reactor satisfies the following conditional expressions.

［実施例］ 下記の組成のＣ４炭化水累混合物である原料を用意した
。[Example] A raw material which is a C4 hydrocarbon mixture having the following composition was prepared.

イソブタン　　　　　　　　０．０３　　小早％ノルマ
ルブタン　　　　　１７．２２　　７／−イソブテン　
　　　　　　　６．９０　　　／／ブテンー１　　　　
　　　４６．６２　　　／／１−ランスブテン−２１７
，４５／／ シスブテンー２　　　　　１０．８９　　　／／１．３
ブタジエン　　　　　０．７４２／／１．２ブタジエン
　　　　　０．１４８／／エヂルアセヂレン　　　　１
０重ｆｉ％ｐｐｍビニルアレチレン　　　　１０／／ この原料中のジｌン類およびアセチレン類の水素添加に
必要な化学量論的水素量は、濃度にして３３２．５重量
１’ｌｐｍである。Isobutane 0.03 Kohaya%N-butane 17.22 7/-isobutene
6.90 //Butene-1
46.62 //1-Lanthbutene-217
,45// Cisbutene-2 10.89 //1.3
Butadiene 0.742//1.2 Butadiene 0.148//Edylacetylene 1
0wt% ppm vinyl alethylene 10// The stoichiometric amount of hydrogen required for hydrogenation of the dienes and acetylenes in this raw material is 332.5wtlpm in terms of concentration.

この原料は、あらかしめ低沸魚介を蒸留分離したもので
あり、これを水添異性化反応装置に供給した。　反応装
置はアルミナ単体にパラジウムを０．５重量％担持させ
た触媒を充填した２基の反応器からなり、第１段反応器
は１５００文、第２段の反応器は４００Ｊ２の容量をも
つ。　水素の過剰率を１５０〜１８００％、反応温度を
２０〜３２°０、圧力を１１〜１７Ｋｇ／Ｃｌｎ２Ｇの
範囲で変化さけて水添異性化を行なった。　最後に、水
添異性化反応生成物に含イｊされているわ、沸分を蒸留
により分離除去した。　反応条件、水添異性化反応生成
物の組成および最終製品中のイソブチレンの温度を表に
まとめて示づ。This raw material was obtained by distilling and separating low boiling point seafood, and was supplied to the hydroisomerization reactor. The reactor consists of two reactors filled with a catalyst in which 0.5% by weight of palladium is supported on alumina alone, the first stage reactor having a capacity of 1500 J2, and the second stage reactor having a capacity of 400 J2. Hydroisomerization was carried out while changing the hydrogen excess rate from 150 to 1800%, the reaction temperature from 20 to 32°0, and the pressure from 11 to 17 Kg/Cln2G. Finally, the boiling matter contained in the hydroisomerization reaction product was separated and removed by distillation. The reaction conditions, the composition of the hydroisomerization reaction product, and the temperature of isobutylene in the final product are summarized in a table.

表のデータから、化学量論的所要水素）農度に対する過
剰率が高くなるほどブテン−１の異性化転化率が高くな
ることがわかる。　実施例３おＪ：びｂで得た、水添異
性化反応物から高沸分を除去して得た留出物中のイソブ
チレン濃度約４５重量％は、ＢＢ留分からイソブチレン
を除去しｌ、：　Ｓ　［３Ｂ留分中のイソブチレン淵１
良と【Ｊぼ同等であり、−１゛ＢＡ合成原籾として十分
使用可能である。From the data in the table, it can be seen that the higher the excess relative to the stoichiometric hydrogen requirement, the higher the isomerization conversion of butene-1. Example 3 J: The isobutylene concentration in the distillate obtained by removing high-boiling components from the hydrogenated isomerization reaction product obtained in steps 3 and 2 and b is approximately 45% by weight. : S [Isobutylene edge 1 in 3B fraction
It is equivalent to good and [J], and can be fully used as -1゛BA synthetic raw rice.

まＩＣ、水添巽性化反応によってイソブチレンは消費さ
れることはなく、むしろ増加していることもわかる。It can also be seen that isobutylene is not consumed by the IC hydrogenation reaction, but rather increases.

一方、水素過剰率か低くなって本５ト明の条イ！１を満
たさなくなると、ブテン−１の異性化添加率は大幅に低
下している。On the other hand, the hydrogen excess rate has decreased and this is a major problem! 1 is no longer satisfied, the isomerization addition rate of butene-1 decreases significantly.

本発明の方法においでは、反応温度および圧力は、反応
生成物の組成に（Ｊとんど影響を与えないこともわかっ
た。It has also been found that in the process of the invention, the reaction temperature and pressure have little effect on the composition of the reaction products.

反応ｆｉｊ＊ｆｉ（℃）　　　０４炭化　　水素流１ｉ
ｔ（Ｎｎ３／ｈｒ）　　　水素Ｎｏ　　　反応圧力　　
第１段　第２段　　水素７Ｍ（’Ｉ　　　　第１段　　
　第２段　　過剰率Ｋｇ／ｃＭＧ　　反応器　反応器　
　Ｋす／１）ｒ　　　　反応器　　　反応器　　（％）
実施例１　　１１　　　　２２　　２０　　２３００　
　　８０．’２　　４．８　　　９００実施Ｍ２　　１
２　　　　２２　　２０　　２３００　　１２２．７　
　４．８　　１４００実施例３　　１５　　　　２２　
　２０　　２３００　　１５６．６　　４．８　　１８
００実１ｈ例４　　１１　　　　２２　　２０　　３２
５０　　１１３．０　　６．８　　　９００実施例５　
　１５　　　　２２　　２０　　３２５０　　２２１．
３　　６．８　　１８００１実施例６　　１１　　　　
３２　　３０　　２３００　　１２２．７　　４．８　
　１４００実施例７　　１７　　　　２２　　２０　　
２３００　　１２２．７　　４．８　　１４．００比較
例１　　１１　　　　２２　　２０　　３２５０　　　
　／１３．５　　４．り　　　　３００比較例２１１２
２２０　３２５０　　　２７．５　　２．５　　　１５
０比較例３　　１１　　　　２２　　２０　　６５００
　　　５５．２　　４．８　　　１５０１Ｂ・・イソブ
ヂレン　　ＢＤ・ブタジェン　　「△・エチルアセチレ
ン　　Ｖ水素転化反応生成物　　　　　　　　　　　　
　　ｒ３−１　　　最終生成物中＋Ｂ　　Ｌ３ＢＤ　　
Ｉ、２ＢＤ　　　ＥＡ　　　　ＶＡ　　　　Ｂ−１転化
率ノｌ　Ｂｆａｌｆｆ中Ｑｊ％　　　　　　　　重量（
ｐｐｍ　）　　　　　　　　　千吊％　　　　〈％）　
　　　重量％６９２　５↓　　５↓　　　５１　　　５
↓　　２７．９３　　７ＩＯ，０９１９，８４７，６１
／／　　　　／／　　　　　／／　　　　　）／　　　
　１７．６２　　　Ｇ２．２１　　　３０．１３７．５
９　　　／／　　　　ｉｉ　　　　　／／　　　　　／
／　　　　　９．３７　　７９．９０　　　４４．６７
６．９３　　　／／　　　　／／　　　　　ｌ／　　　
　　／／　　　　２７．９０　　４０．１５　　．１９
，８８７．５ｇ　　　／／　　　　／／　　　　　／／
　　　　　／／　　　　　９．３４　　７９．９６　　
　　’Ｉ’！、７５７．４１　　　／／　　　　／／　
　　　　／／　　　　　／／　　　　１７．６７　　６
２．１０　　　２９．５１７．４５　　　ｉｉ　　　　
ｉｉ　　　　　〃ｔｙ　　　　１７．６５　　６２．１
５　　　２９．６５６．９９　　　Ｊ／　　　　／／　
　　　　ｌ／　　　　　／／−４０，３０１３，５５１
４，７７７，１０４０，１０／／　　　　　ｒｉ　　　
　４３．３９　　　６．９２　　　１４．０５６．８６
　　８０　　２５　　　　／／　　　　　／／　　　　
４３．３９　　　６．９２　　　１３．６４Ａ・・ビニ
ルアヒジエン　　Ｂ・・ステン発明の効宋 本発明の方法にＪこれば、Ｃ４炭化水素混合物中のイソ
ブヂレンの濃縮を効果的に７−テなって高い回収率でこ
れを冑ることができる。　この方法は、どくに０ｉ）斜
中のイゾブジエン温度が低い場合に、その意義が大きい
。Reaction fij * fi (℃) 04 Hydrocarbon Hydrogen flow 1i
t(Nn3/hr) Hydrogen No Reaction pressure
1st stage 2nd stage Hydrogen 7M ('I 1st stage
2nd stage Excess rate Kg/cMG Reactor Reactor
Ksu/1)r Reactor Reactor (%)
Example 1 11 22 20 2300
80. '2 4.8 900 implementation M2 1
2 22 20 2300 122.7
4.8 1400 Example 3 15 22
20 2300 156.6 4.8 18
00 Actual 1h Example 4 11 22 20 32
50 113.0 6.8 900 Example 5
15 22 20 3250 221.
3 6.8 18001 Example 6 11
32 30 2300 122.7 4.8
1400 Example 7 17 22 20
2300 122.7 4.8 14.00 Comparative example 1 11 22 20 3250
/13.5 4. 300 Comparative Example 2112
220 3250 27.5 2.5 15
0 Comparative Example 3 11 22 20 6500
55.2 4.8 1501B... Isobutylene BD Butadiene "△ Ethylacetylene V Hydrogen conversion reaction product
r3-1 +B L3BD in final product
I, 2BD EA VA B-1 Conversion rate No. Qj% in Bfalff Weight (
ppm) Thousand hanging% (%)
Weight%692 5↓ 5↓ 51 5
↓ 27.93 7IO,0919,847,61
／／ ／／ ／／ )／
17.62 G2.21 30.137.5
9 // ii // /
/ 9.37 79.90 44.67
6.93 // // l/
// 27.90 40.15. 19
,887.5g // // // //
// 9.34 79.96
'I'! , 757.41 // //
// // 17.67 6
2.10 29.517.45 ii
ii 〃ty 17.65 62.1
5 29.656.99 J/ //
l///-40,3013,551
4,777,1040,10//ri
43.39 6.92 14.056.86
80 25 // //
43.39 6.92 13.64 A...Vinylahidiene B...Effects of the Sten Invention The method of the present invention can effectively concentrate isobutylene in a C4 hydrocarbon mixture with a high recovery rate. You can get rid of this. This method has great significance when the temperature of isobudiene in the solution is low.

Claims (5)

【特許請求の範囲】[Claims] （１）Ｃ＿４炭化水素中のイソブチレンを濃縮する方法
において、Ｃ＿４炭化水素を水添異性化触媒を充填した
反応器に水素を添加しながら供給してＣ＿４炭化水素中
のブテン−１をブテン−２に異性化する水添異性化工程
、低沸分を除去する蒸留分離工程および高沸分を除去す
る蒸留分離工程からなり、上記の水添異性化工程を、Ｙ
≧Ｚ（Ｘ＋４．１４）／４．４２３×０．５Ｙ：水素量
（モル数） Ｘ：ブテン−１の転化率（％） Ｚ：Ｃ＿４炭化水素中のジエン類およびアセチレン類の
総モル数 の関係式を満足する量の水素の添加の下に実施すること
を特徴とする方法。(1) In a method for concentrating isobutylene in C_4 hydrocarbons, C_4 hydrocarbons are supplied to a reactor filled with a hydroisomerization catalyst while adding hydrogen, and butene-1 in C_4 hydrocarbons is converted to butene-2. It consists of a hydrogen isomerization step to isomerize to Y, a distillation separation step to remove low boiling components, and a distillation separation step to remove high boiling components.
≧Z(X+4.14)/4.423×0.5Y: Hydrogen amount (number of moles) X: Conversion rate of butene-1 (%) Z: Total number of moles of dienes and acetylenes in C_4 hydrocarbon A method characterized in that the method is carried out while adding an amount of hydrogen that satisfies the relational expression. （２）はじめに低沸分を除去する蒸留分離工程、ついで
水添異性化工程、そして高沸分を除去する蒸留分離工程
、の順で実施する特許請求の範囲第１項に記載の方法。(2) The method according to claim 1, which is carried out in the following order: first, a distillation separation step for removing low-boiling components, then a hydroisomerization step, and then a distillation separation step for removing high-boiling components. （３）複数の水添異性化反応器を直列に接続して使用し
、各反応器に水素を添加しながら水添異性化を行なう特
許請求の範囲第１項または第２項に記載の方法。(3) The method according to claim 1 or 2, which uses a plurality of hydroisomerization reactors connected in series and performs hydroisomerization while adding hydrogen to each reactor. . （４）不活性アルミナを担体とし、これにパラジウムを
０．１〜３．０重量％担持させた水添異性化触媒を使用
する特許請求の範囲第１項または第２項に記載の方法。(4) The method according to claim 1 or 2, which uses a hydroisomerization catalyst in which inert alumina is used as a carrier and palladium is supported in an amount of 0.1 to 3.0% by weight. （５）反応温度を０〜１００℃、圧力を５〜５０Ｋｇ／
ｃｍ＾２Ｇとし、反応系を液相に保って実施する特許請
求の範囲第１項または第２項に記載の方法(5) Reaction temperature 0~100℃, pressure 5~50Kg/
cm^2G, and the method according to claim 1 or 2, which is carried out by keeping the reaction system in a liquid phase.
JP59140383A 1984-07-06 1984-07-06 Concentration of isobutylene in c4 hydrocarbons Pending JPS6118732A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP59140383A JPS6118732A (en) 1984-07-06 1984-07-06 Concentration of isobutylene in c4 hydrocarbons

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
JP59140383A JPS6118732A (en) 1984-07-06 1984-07-06 Concentration of isobutylene in c4 hydrocarbons

Publications (1)

Publication Number Publication Date
JPS6118732A true JPS6118732A (en) 1986-01-27

Family

ID=15267533

Family Applications (1)

Application Number Title Priority Date Filing Date
JP59140383A Pending JPS6118732A (en) 1984-07-06 1984-07-06 Concentration of isobutylene in c4 hydrocarbons

Country Status (1)

Country Link
JP (1) JPS6118732A (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2757506A1 (en) * 1996-12-23 1998-06-26 Inst Francais Du Petrole PROCESS FOR PRODUCING HIGH PURITY ISOBUTENE COMBINING REACTIVE HYDROISOMERIZATION DISTILLATION AND SKELETTAL ISOMERIZATION
FR2757505A1 (en) * 1996-12-23 1998-06-26 Inst Francais Du Petrole PROCESS FOR THE PRODUCTION OF HIGH PURITY ISOBUTENE COMBINING REACTIVE HYDROISOMERIZATION DISTILLATION, DISTILLATION AND SKELETTAL ISOMERIZATION
JP4773012B2 (en) * 1999-07-16 2011-09-14 キャタリティック・ディスティレイション・テクノロジーズ Process for separating isobutene from normal butenes

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2757506A1 (en) * 1996-12-23 1998-06-26 Inst Francais Du Petrole PROCESS FOR PRODUCING HIGH PURITY ISOBUTENE COMBINING REACTIVE HYDROISOMERIZATION DISTILLATION AND SKELETTAL ISOMERIZATION
FR2757505A1 (en) * 1996-12-23 1998-06-26 Inst Francais Du Petrole PROCESS FOR THE PRODUCTION OF HIGH PURITY ISOBUTENE COMBINING REACTIVE HYDROISOMERIZATION DISTILLATION, DISTILLATION AND SKELETTAL ISOMERIZATION
EP0850903A1 (en) * 1996-12-23 1998-07-01 Institut Francais Du Petrole Process for the preparation of very pure isobutene combining a reactive distillation hydroisomerisation and an isomerisation of the carbon skeleton
EP0850904A1 (en) * 1996-12-23 1998-07-01 Institut Francais Du Petrole Process for the preparation of very pure isobutene combining a reactive distillation hydroisomerisation, a distillation and a carbon skeleton isomerisation
JP4773012B2 (en) * 1999-07-16 2011-09-14 キャタリティック・ディスティレイション・テクノロジーズ Process for separating isobutene from normal butenes

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