СПОСОБ АЛКИЛИРОВАНИЯ С ПОВТОРНЫМ ВЗАИМОДЕЙСТВИЕМ В РЕЗЕРВУАРЕ ДЛЯ ОТСТАИВАНИЯ

Изобретение может быть использовано в химической промышленности. Система для алкилирования олефинов парафином включает реактор алкилирования 100 и резервуар для отстаивания 110, имеющий верхнюю часть 122, промежуточную часть 108 и нижнюю часть 124. Промежуточная часть 108 содержит по меньшей мере одну систему тарелок 112, содержащую перфорированную тарелку 114, содержащую множество отверстий 116 и слой насадки 118, расположенный ниже указанной перфорированной тарелки 114. Углеводородное исходное сырье подают в реактор алкилирования 100 через трубопровод подачи 104. Резервуар для отстаивания 110 функционально связан с реактором алкилирования 100 по потоку текучей среды через трубопровод питания 106. Изобретение позволяет снизить концентрацию органических фторидов в продукте алкилирования. 2 н. и 19 з.п. ф-лы, 2 табл., 8 ил.

VERFAHREN UND EINRICHTUNG ZUR STEUERUNG EINER ALKYLIERUNGSANLAGE

ISOPARRAFIN-OLEFIN-ALKYLIERUNG

Improvements relating to the production of motor fuels

... 526,165. Hydrocarbons. ANGLO-IRANIAN OIL CO., Ltd., DUNSTAN. A. E., and BIRCH, S. F. Feb. 3, 1939, No. 3685. [Class 2 (iii)] Gasoline hydrocarbons are prepared by reacting isobutane or isopentane with ethylene in the presence of concentrated sulphuric acid containing cupric sulphate and mercurous sulphate. The reaction is preferably effected in the liquid phase at a temperature of-10‹C. to 60‹C., superatmospheric pressure being necessary in the case of isobutane. The isoparaffin is present in substantial excess and the mixture is vigorously stirred. Since iron exerts an inhibiting effect upon the reaction, the apparatus is made of other materials than iron and mild steel. An example is given of the alkylation of isopentane with ethylene. Specification 515,039 is referred to.

Improvements in or relating to manufacture of motor fuel

... 526,149. Synthetic motor spirit. TEXACO DEVELOPMENT CORPORATION. March 9, 1939, No. 7648. Convention date, March 18, 1938. [Class 2 (iii)] In producing gasoline of high octane number by alkylating isobutane with normally gaseous olefines heavier than ethylene in presence of strong sulphuric acid, the normally gaseous hydrocarbons separated from the normally liquid reaction products are fractioned to obtain a portion rich in isobutane which is recycled to the alkylation operation, and the total weight of isobutane, including that recycled, is at least 3 times that of the olefines. Advantageously, normal butane separated is combined with the gasoline to increase its volatility. The olefines may be C or C 4 cracked hydrocarbon fractions, the acid is 80-100 per cent. H 2 SO 4 and at least equal in weight to the olefines ; the temperature -40 to + 176‹F. ; and the pressure is normally sufficient to keep the hydrocarbons liquid e.g. 25-150 lb. For example, unsaturated C 4 hydrocarbon stock in ...

An improved manufacture of normally liquid hydrocarbons by alkylation

... 539,480. Acyclic hydrocarbons. STANDARD OIL DEVELOPMENT CO. Nov. 13, 1939, Nos. 29936 and 29937. Convention dates, Dec. 7, 1938, and Dec. 30,1938. [Class 2 (iii)] The reaction of an isoparaffin with a mono-olefine for the production of a safety fuel is conducted in the presence of those constituents of the product which it is desired to suppress, and which boil above and below the boiling point of the desired fraction. Thus the product may be fractionated to give a fraction of predominantly C 5 -C 7 hydrocarbons, another of predominantly C 8 -C 12 hydrocarbons and a third of C 13 and heavier hydrocarbons, the first and third fractions being recycled to the alkylation zone. In an example, a feed stock comprising mainly isobutylene and isobutane is reacted in the presence of a C 5 -C 7 fraction and also a C 9 and heavier fraction obtained from a previous alkylation. For continuous operation the apparatus shown in the Figure is suitable. The mono-olefin-isoparaffin mixture is compressed and ...

Improvements relating to the production of motor fuel

An aviation or motor spirit or constituent thereof is obtained by the alkylation of an isoparaffin. Iso-butane or iso-pentane is condensed with an olefine or olefines, e.g. propylene, iso- or n-butene or the lower polymerides thereof, particularly the dimeride and trimeride, in the presence of sulphuric acid at low temperatures, e.g. -10 to + 30 DEG C. and in substantially equimolecular proportions. On settlement, an upper hydrocarbon layer separates, from which the spirit may be produced by distillation. Normal paraffins or inert hydrocarbons may be present, but preferably aromatic hydrocarbons are absent. An excess of the iso-paraffin may be used, and this is stated to increase the yield of the condensate. The reaction is carried out in the liquid phase and if necessary, pressure sufficient to maintain the liquid phase may be used. The iso-paraffin may be mixed with the acid, and the olefine added gradually with vigorous stirring, which may be maintained after all the reactants are mixed ...

Improvements in or relating to alkylation of hydrocarbons

... 515,367. Hydrocarbons ; motor fuel. TEXACO DEVELOPMENT CORPORATION. May 30, 1938, No. 16092. Convention date, June 18; 1937. [Class 2(iii)] Saturated hydrocarbons of gasoline boiling range or higher, suitable for motor fuel are obtained by bringing in liquid phase an excess of low boiling isoparaffins together with olefines into contact with strong sulphuric acid,- separating the alkylation products and recycling at least part of the unreacted isoparaffins. In the Fig., an oienne, e.g. propylene or a cracked gas containing butylenes and an isoparaffin, e.g., isobutane are forced through pipes 3 and 7 respectively into a mixer 4 containing sulphuric acid. The reaction mixture is passed to a separator 18 in order to separate the acid, which may be recycled. The oil which is produced is withdrawn through pipe 34 and passed to a neutralizer 25 containing caustic alkali or other neutralizing agent. The oil, after being allowed to settle in settling tank 33 is passed to a fractionator 41 from ...

An improved manufacture of hydrocarbons by alkylation

... 553,334. Acyclic hydrocarbons. STANDARD OIL DEVELOPMENT CO. July 10, 1940, No. 11488. Convention date, Dec. 28, 1939. [Class 2 (iii)] In a two-stage alkylation process wherein a sulphuric acid extract of olefins is reacted with at least one paraffin containing at least one tertiary carbon atom under alkylation reaction conditions, there are fed to the extraction zone sulphuric acid of alkylating strength, i.e. of 90-110 per cent. concentration, and a mixture containing mono-olefins, in the proportion of about 0.4 to about 1.25 mols. of acid per mol. of mono-olefins. Advantageously, the extract used for the alkylation contains about 0.77 to about 2.5 mols. of acid per mol. of mono-olefin. In an example, a refinery C 4 cut is fed by a pipe 2, Fig. 1, to the extractor 3 provided with a mechanical stirrer 4 and receiving partially spent alkylation acid through a pipe 27 from a settler 26 associated with the alkylation reactor 16 and fresh acid may be supplied to the pipe 27 through pipes 24 ...

PROCESS FOR RECOVERING USED SULPHURIC ACID

... 1,207,138. Alkylating isoparaffins. TEXACO DEVELOPMENT CORP. 15 Dec., 1967 [16 Dec., 1966], No. 57225/67. Heading C5E. In a process wherein an isoparaffin is alkylated with an olefin in the presence of sulphuric acid, and in which used sulphuric acid of non- catalytic concentration (for alkylation) is contacted with an olefin to produce dialky] sulphates in a reaction zone in which the titratable acidity of sulphuric acid is maintained below 80% by wt. H 2 SO 4 , a paraffinic hydrocarbon is introduced simultaneously into the zone in which dialkyl sulphates are formed so as to extract the dialkyl sulphates into the paraffinic hydrocarbon, at least part of the extract then being passed to the alkylation zone. The simultaneous absorption/extraction zone preferably operates in countercurrent.

A process for the production of hydrocarbons

... 540,824. Aliphatic hydrocarbons. NAAMLOOZE VENNOOTSCHAP DE BATAAFSCHE PETROLEUM MAATSCHAPPIJ. Dec. 8, 1939, Nos. 31807 and 31808. Convention dates, Dec. 14, 1938, and May 27, 1939. [Class 2 (iii)] Olefines having at least six carbon atoms in the molecule are continuously fed into a circulating dispersion of isoparaffin and 85 to 110 per cent sulphuric acid at such a rate that the molar ratio of isoparaffins to olefines in the dispersion at the point of introduction of the olefines is at least 2:1, a portion of the dispersion is continuously withdrawn at a point where substantially no olefines remain unreacted, the desired hydrocarbon products are removed from the dispersion thus withdrawn and the unreacted isoparaffins are returned to the circulating dispersion. The reaction is conducted at 50-20 to 50‹C. and the olefines are advantageously diluted with isoparaffins before their introduction. In Fig. 1, the isoparaffins and olefines are fed into the system by pipes 1, 2 respectively and ...

Alkylation process

... 559,053. Alkylation process. SHELL DEVELOPMENT CO. May 27, 1942, No. 7180. Convention date, Oct. 11, 1941. [Class 2 (iii)] Alkylatable organic compounds such as isoparaffins, cyclopentanes, cyclohexanes, aromatic hydrocarbons, phenols, cresols, aniline, nitrobenzene, and halobenzenes, are alkylated with a normally liquid olefine capable of forming an active oxygen-containing compound which tends to shorten the life of the alkylation catalyst, the alkylation taking place in the substantial absence of said active oxygencontaining compound. Its absence may be obtained by adding an antioxidant such as a naphthol, tertiary butyl phenol or cresol, or resorcinol, to the olefine, or distilling the olefine to obtain a fraction having a lower concentration of said oxygen-containing compound, or by treating the olefine with reducing agents such as sodium bisulphite or by using an oxalic acid-sulphuric acid mixture. The olefine used is preferably a polymer of a lower boiling olefine, such as ethylene ...

Isoparaffin-olefin alkylation process

A process for the acid-catalyzed alkylation of an isoparaffinic hydrocarbon with an olefinic hydrocarbon is disclosed. The alkylation is effected at alkylation reaction conditions resulting in an alkylation reaction mixture containing a vapor phase generated by the exothermic heat of reaction. The vapor phase so generated has a cooling effect permitting the alkylation reaction to be effected at lower temperatures more conducive to higher quality alkylation product.

Acid catalyst separation in emulsion alkylation of olefins with isoparaffins

In the emulsion alkylation of an isoparaffin with an olefine using a liquid acid catalyst which constitutes more than 50 per cent by volume of the emulsion, emulsion is continuously withdrawn to an agitated emulsion modifying zone where sufficient hydrocarbon is added from an emulsion breaking zone in side-by-side relationship therewith to reduce the acid content to 10-30 per cent by whence the emulsion passes to said non-agitated emulsion breaking zone, acid being recycled to the reaction zone and a portion of the upper hydrocarbon layer being returned to the emulsion modifying zone. In a preferred embodiment emulsion enters the settler by inlet 31 and so enters the stirred modifying zone. Hydrocarbon also passes into the modifying zone from the primary settling zone overflowing the adjustable weirs 42. Modified emulsion passes to the primary settling zone by two holes 39 (Fig. 5) in front of which are two baffles ...

Process of catalytic hydrocarbon alkylation.

Process of isoparaffin alkylation.

Process of condensation of a matter alcoylable with a compound with olefinic reaction.

PROCEDURE AND DEVICE FOR THE PRODUCTION OF ALKYLATES

PROCEDURE FOR THE DISTANCE OF WATER FROM A ALKYIERUNGSPROZESSSYSTEM

PROCEDURE FOR THE CATALYTIC ALKYLATION OF ISO BUTANE WITH A OLEFIN

ALKYLATING DEVICE AND PROCEDURE FOR THE ISOLATION OF THE CATALYST

VERFAHREN ZUR KATALYTISCHEN ALKYLIERUNG VON ISOBUTAN MIT EINEM OLEFIN

ALKYLATING PROCEDURE.

POLLUTION FREE CATALYTIC ALKYLATION WITH THE HELP OF LIQUID ONIUM POLYHYDROGENFLUORIDEN

METHOD AND APPARATUS FOR SEPARATING IMMISCIBLE FLUIDS IN ALKYLATION PROCESS

ALKYLATION OF PARAFFINIC HYDROCARBONS USING ACIDIC CATALYSTS

Method for separating conjunct polymeric byproducts from mixture containing hydrofluoric acid and a sulfolane

LOWER OLEFINS TO LIQUID HYDROCARBONS

Alkylation of olefin hydrocarbons by isoparaffin hydrocarbons with sulfone-HF-H2O catalyst

ALKYLATION OF ISOPARAFFINS AND THE REACTION PRODUCTS OF ISOPARAFFINS AND OLEFINS TO PRODUCE HIGH OCTANE BLENDING STOCKS

Alkylation process

MEANS AND METHOD FOR CONTROLLING AN ALKYLATION UNIT TO ACHIEVE A DESIRED FEED ISOBUTANE RATE

ADAMANTYL CARBOXYLIC AND SULFONIC ACID CATALYZED PARAFFIN-OLEFIN ALKYLATION AND PARAFFIN ISOMERIZATION

PROCESS FOR THE ALKYLATION OF LIGHT PARAFFINS WITH LOWER OLEFINS

Alkylates are prepared by selectively alkylating light paraffinic hydrocarbons with lower olefins at alkylation conditions in the presence of a substantially liquid phase catalyst comprising (a) one or more Lewis acids of the formula MXn where M is selected from the Group IIIA, IVB, V or VIB elements of the Periodic Table, X is a halogen, n is the ratio of halogen atoms to atoms of M and varies from 1-8, and (b) a hydrogen halide.

CATALYTIC ALKYLATION PROCESS

... (4888 A) IMPROVED CATALYTIC ALXYLATION PROCESS In the process for the catalytic alkylation of isobutane with an olefin to produce alkylate, the liquid reactor effluent stream comprising a hydrocarbon mixture of alkylate, isobutene and inert alkanes is used to provide cooling to the various condensers in the alkylation process.

CONTROL OF AN ALKYLATION REACTOR

An acid alkylation process is controlled so as to maintain a desired ratio of isobutane to olefins in a fluid stream flowing to the alkylation reactor and to maintain a desired acid to hydrocarbon ratio in the alkylation reactor. Also, if parallel alkylation reactors are utilized, the flow rate of the olefin stream to one of the alkylation reactors is manipulated so as to maintain a balanced loading on the parallel alkylation reactors. Such control results in improved quality of the alkylate produced and also improves the amount of alkylate produced from a particular amount of fluid to the alkylation reactor.

HF ALKYLATION OF ISOPARAFFIN WITH OLEFIN HEAVIER THAN ETHYLENE WITH ETHYL FLUORIDE AS REACTION IMPROVER

ISOPARAFFIN-OLEFIN ALKYLATION

This invention relates to a process for effecting alkylation of an isoparaffin with an olefin in the presence of a catalyst comprising a macroreticular acid cation exchange resin characterized by a surface acid concentration of less than about 0.5 milliequivalents of hydrogen ion per square meter surface area and boron trifluoride, the latter being present in an amount in excess of that required to saturate said resin.

MOTOR FUEL ALKYLATION CATALYST AND PROCESS FOR THE USE THEREOF

... "NOVEL MOTOR FUEL ALKYLATION CATALYST AND PROCESS FOR THE USE THEREOF" A novel hydrocarbon alkylation catalyst is disclosed comprising a mineral acid and an ether component. A process for utilizing the novel catalyst is also disclosed.

CONTROL TECHNIQUE FOR CONVERSION OF OXYGENATES TO LIQUID HYDROCARBONS

CONTROL TECHNIQUE FOR CONVERSION OF OXYGENATES TO LIQUID HYDROCARBONS A process control technique for upgrading C3-C4 hydrocarbon feed containing olefins to produce heavier liquid hydrocarbons comprising converting a major portion of C3-C4 olefins in an oligomerization zone by contacting a shape selective medium pore zeolite catalyst at elevated temperature and pressure to make distillate and olefinic gasoline. The oligomerization stage effluent is fractionated to provide distillate and gasoline product and a C3-C4 intermediate stream containing isobutane and unconverted propene and butylene. The C3-C4 intermediate stream is combined under control with a portion of C3-C4 feed and further converting the combined streams in an alkylation zone to make heavier paraffinic hydrocarbons. The olefin feed may be produced by catalytically converting methanol or similar oxygenated hydrocarbons in a known process. Controlled material balance is achieved by accumulating liquid olefin feed to the oligomerization ...

CATALYTIC COMPOSITION FOR THE CONVERSION OF HYDROCARBONS

ALKYLATION PROCESS UTILIZING HYDROFLUORIC ACID WITH A MINOR AMOUNT OF FLUOROSULFURIC ACID

ALKYLATION PROCESS WITH SETTLER EFFLUENT RECYCLE

METHOD FOR REDUCING ORGANIC FLUORIDE LEVELS IN HYDROCARBONS

A system and/or process for decreasing the level of at least one organic fluoride present in a hydrocarbon mixture (118) by first passing the hydrocarbon mixture (118) to an eductor (120) and educting into the hydrocarbon mixture a catalyst (122) comprising a volatility reducing additive and hydrofluoric acid to produce a hydrocarbon-catalyst mixture (132), permitting the hydrocarbon-catalyst mixture (132) to undergo a phase separation to produce a hydrocarbon phase (128) having a lower concentration of at least one organic fluoride than the hydrocarbon mixture (132) and to produce a catalyst phase (130), and withdrawing at least a portion of the hydrocarbon phase to thereby form a hydrocarbon product stream (134), are disclosed. In an alternate embodiment, a system and/or process for controlling the concentration of at least one organic fluoride and/or the RON of the hydrocarbon mixture by adjusting the amount of the volatility reducing additive present in the catalyst are disclosed.

PRODUCTION OF ISO-OCTENE FROM TERTIARY ALCOHOLS

Systems and methods are provided for forming alkylate from a tertiary alcohol feed. Olefins for the alkylation reaction can be generated from a portion of the tertiary alcohol feed. The tertiary alcohol feed can be obtained, for example, by selective oxidation to convert a portion of an isoparaffin-containing feed into alcohol, such as conversion of isobutane to t-butyl alcohol. The alcohol can then be converted to an alkene, such as conversion of t-butyl alcohol to isobutene, in the alkylation reaction environment in the presence of a solid acid catalyst. The solid acid catalyst can then facilitate dimerization of the alkenes (e.g. isobutene) to form C8+ olefins (e.g. isooctene). A catalyst having an MWW framework is an example of a suitable solid acid catalyst.

PRODUCTION OF HIGH OCTANE HYDROCARBON FROM ISOBUTANE VIA TERT-BUTANOL

Systems and methods are provided for production of high octane hydrocarbon from an isoparaffin feed using oxidation acid catalysis chemistry.

PARAFFIN ALKYLATION PROCESS

A process for the alkylation of isobutane is disclosed wherein isobutane is fed to two separate alkylation systems. The effluent from the first alkylation system is fed to an interim debutanizer where the C4's are separated from the alkylate product. The overhead C4 product is then fed to the second alkylation system to provide the isobutane. The effluent from the second alkylation system is fed to a traditional deisobutanizer to prevent any build up of normal butanes in the system.

ENVIRONMENTALLY SAFE CATALYTIC ALKYLATION USING LIQUID ONIUM POLY(HYDROGEN FLUORIDES)

PARAFFIN ALKYLATION CATALYST

Catalyseur à base de silice et d'acide sulfurique et son utilisation en alkylation calalytique d'isobulane et/ou d'isopentane en présence d'au moins une oléfine comportant de 3 à 6 atomes de carbone par molécule.

ISOPARAFFIN-OLEFIN ALKYLATION

A novel alkylation catalyst is described which is used in processes for alkylating olefin hydrocarbons with isoparaffin hydrocarbons to produce high octane alkylate products suitable for use as a blending component of gasoline motor fuel. The novel catalyst comprises a mixture of an anhydrous hydrogen halide and a sulfone. The novel alkylation catalyst is utilized in a novel process for alkylating olefin hydrocarbons with isoparaffin hydrocarbons.

Alkylation Process and Catalyst Therefor

Transfer of Catalyst

ALKYLATION PROCESS USING HYDROGEN FLUORIDE-CONTAINING ALKYLATION CATALYSTS

A feedstock is alkylated in presence of a hydrogen fluoride containing catalyst, which also comprises a carrier. Possible carriers are: a synthetic water soluble polymer like sodium acrylate or a salt like ammonium trifluoroacetate, ammonium sulfate or ammonium methanesulfonate.

REGENERATION OF HYDROGEN FLUORIDE ALKYLATION CATALYST

An improved process for the regeneration of an ASO-containing HF catalyst by the removal of ASO from said catalyst through the utilization of a separation column.

Verfahren zur Alkylierung von Paraffinkohlenwasserstoffen

Verfahren zum Alkylieren von alkylierbaren Kohlenwasserstoffen

Verfahren zur Herstellung alkylierter Kohlenwasserstoffe

Alkylierungsverfahren

Verfahren zur Alkylierung eines Isoparaffins

Verfahren zur Alkylierung von Paraffinkohlenwasserstoffen

Verfahren zur Alkylierung von Isobutan

METHOD AND DEVICE FOR PRODUCING ALKILATOV

SYSTEM AND THE METHOD OF THE ALKYLATION OF THE HYDROCARBON

СПОСОБ АЛКИЛИРОВАНИЯ ОЛЕФИНА ИЗОПАРАФИНОМ И УСТАНОВКА ДЛЯ ЕГО ОСУЩЕСТВЛЕНИЯ (ВАРИАНТЫ)

Описаны установка (варианты) и способ алкилирования для повышения отношения изобутана к олефину в способе/установке алкилирования (10). Установка и/или способ включают средства изменения части исходного потока резервуара для отстаивания (119) как материала (123, 125), который подают по крайней мере в одну реакционную зону (101b) ниже по потоку из первой реакционной зоны (101а) многозонального реактора алкилирования (101), вместе с частью олефина, который подают в многозональный реактор алкилирования.

ПРОЦЕСС АЛКИЛИРОВАНИЯ С РЕЦИКЛОМ ВЫХОДНОГО ПОТОКА ИЗ РЕЗЕРВУАРА ДЛЯ ОТСТАИВАНИЯ

Описаны система и/или процесс для повышения отношения изобутана к олефину в процессе/системе алкилирования (10). Система и/или процесс включает средства изменения части выходного потока резервуара для отстаивания (119) как подаваемого материала (123, 125) по крайней мере в одну реакционную зону (101b) ниже по потоку из первой реакционной зоны (101а) многозонального реактора алкилирования (101) вместе с частью олефина, подаваемого в многозональный реактор алкилирования.

СПОСОБ ПОЛУЧЕНИЯ АЛКИЛБЕНЗИНА И РЕАКТОР СЕРНОКИСЛОТНОГО АЛКИЛИРОВАНИЯ ИЗОБУТАНА ОЛЕФИНАМИ

Предложенное изобретение относится к способу (двум вариантам) получения алкилбензина путем алкилирования изобутана олефинами, а также реактору (два варианта) для осуществления предложенного способа. Первый вариант реактора включает реакционную камеру, состоящую из вертикально расположенного цилиндрического корпуса и соосной ему циркуляционной трубы, узлы ввода серной кислоты и циркулирующих продуктов реакций, где узел ввода серной кислоты выполнен в виде камеры с вводным штуцером, размещенным под циркуляционной трубой с торцевым зазором к ней и отделенной от нее поперечной перегородкой, в которой закреплены сопла для ввода серной кислоты в циркуляционную трубу, направленные вверх и размещенные по окружности с диаметром, меньшим внутреннего диаметра циркуляционной трубы, а узел ввода циркулирующих продуктов реакции в смеси с олефиносодержащим сырьем выполнен в виде кольцевой камеры с входным штуцером, размещенной над циркуляционной трубой и снабженной соплами, направленными вниз и размещенными ...

СПОСОБ И УСТРОЙСТВО ДЛЯ ПОЛУЧЕНИЯ АЛКИЛАТОВ

... 1. Способ получения алкилата(ов) путем серно-кислотного алкилирования, по меньшей мере, одного изопарафина, по меньшей мере, одним олефином, предусматривающий: (a) приготовление смеси указанного, по меньшей мере, одного изопарафина с рециркулируемыми продуктами реакции посредством смешения указанного, по меньшей мере, одного изопарафина, предварительно охлажденного до температуры не выше +12°C, с рециркулируемыми продуктами реакции, отделенными от серной кислоты и также охлажденными до температуры не выше +12°C; (b) приготовление первой эмульсии “углеводороды в кислоте” путем ввода смеси, полученной на стадии (a), множественными параллельными струями в серно-кислотную композицию; (c) приготовление второй эмульсии путем ввода спутными струями через форсунки части указанного, по меньшей мере, одного олефина в первую эмульсию “углеводороды в кислоте”, полученную на стадии (b); (d) ввод второй эмульсии, полученной на стадии (c), через сопла в реакционную камеру с заданной высотой и поперечным ...

СИСТЕМА И СПОСОБ АЛКИЛИРОВАНИЯ УГЛЕВОДОРОДА

Способ алкилирования углеводородов, включающих по крайней мере один изопарафин и по крайней мере один олефин, посредством введения жидкого кислотного катализатора и углеводорода в реактор высокой скорости сдвига, образования эмульсии, содержащей капельки, включающие углеводород, в дисперсной кислотной фазе, в которой капельки имеют средний диаметр менее примерно 5 мкм, введения эмульсии в резервуар, работающий в подходящих для алкилирования условиях, в котором по крайней мере часть изопарафина алкилируется олефином с образованием продукта алкилирования, и выведения потока продукта, включающего продукт алкилирования, из резервуара. Также раскрывается система для выполнения данного способа.

Method for Liquid Phase Alkylation of Olefin

Reactor and use of such a reactor is alkylation reaction method

本发明提供了一种用于至少两种液态物料的反应器，包括：封闭式的反应器壳体；进料管，其具有用于分别接受各液态物料的相应入口；分配管，其与进料管连通并延伸到反应器壳体内，并且在延伸到反应器壳体内的区域中设有若干分配孔；空心柱体形式的旋转床，其通过固定机构安装于反应器壳体内，从而将反应器壳体的内腔分成中心区和外侧区，旋转床能够在驱动机构的带动下旋转；以及设于反应器壳体的下部的用于输出反应后物料的出料口。其中，分配管与旋转床的内表面间隔开地伸入到中心区内，使得物料能够从中心区穿过旋转床而进入外侧区，并且经由出料口输出。

A method for carrying out chemical reactions using fractions rich in propylene and coming from the hydrocarbon pyrolysis

PROCEDE PERFECTIONNE D'ALKYLATION AVEC CATALYSEUR HF

L'INVENTION A POUR OBJET UN PROCEDE D'ALKYLATION CATALYSE PAR HF D'UNE ISOPARAFFINE AVEC UNE CHARGE OLEFINIQUE. ON SEPARE L'ISOPARAFFINE DE LA N-PARAFFINE DANS UNE ZONE DE SEPARATION, DANS DES CONDITIONS PERMETTANT D'OBTENIR UN CONCENTRE D'ISOPARAFFINE ET UN CONCENTRE DE N-PARAFFINE; ON FAIT REAGIR L'ISOPARAFFINE A L'INTERIEUR D'UN REACTEUR 5 AVEC LE COURANT OLEFINIQUE 2 EN MELANGE AVEC LE CATALYSEUR HF DANS DES CONDITIONS PERMETTANT D'OBTENIR UN ALKYLAT NORMALEMENT LIQUIDE, ON INTRODUIT AU MOINS UNE PARTIE LIQUEFIEE DU CONCENTRE DE N-PARAFFINE DANS LE REACTEUR 5 ET ON VAPORISE DANS CELUI-CI LA N-PARAFFINE PAR CONTACT INDIRECT AVEC LE MELANGE DE REACTION D'ISOPARAFFINE ET D'OLEFINE. PRODUCTION D'ALKYLAT POUR CARBURANT MOTEUR.

Paraffin alkylation catalyst

Improvements with the manufacture of fuel for engines

Improvements with the alkylation of hydrocarbons

Process of alkylation of paraffins

PROCEEDED OF PRODUCTION Of GASOLINE HIGH GASOLINE AND OCTANE NUMBER HAS In particular USABLE WITHOUT LEAD FROM OLEFINIC CUTS C3/C4

Paraffin alkylation catalyst.

Improvements with the processes for the alkylation of isoparaffins

Process of hydrocarbon alkylation

Catalytic alkylation of hydrocarbons

Preparation of liquid fuels for engines

Reaction enters the olefins and other hydrocarbons

CATALYSTS SUPERACIDES SUPPORT FOR THE CONVERSION OF HYDROCARBONS

CATALYST SOLIDS Of ALIPHATIC ALKYLATION

L'invention concerne un catalyseur comprenant un support poreux organique ou minéral et au moins une phase active comprenant au moins un acide choisi parmi les acides de formule R-SO3 H, où R est le fluor ou un groupement alkyl ou un groupement alkyl fluoré, et au moins un solvant aprotique organique faiblement basique, ledit support ayant été imprégné par ladite phase active, ledit catalyseur étant tel qu'il est constitué essentiellement de particules de diamètre moyen compris entre 0,1 et 150 mum, et tel que ledit support, avant son imprégnation par ladite phase active, possède un volume poreux total compris entre 0,5 et 6 cm**3/g.

REACTOR AND ALKYLATION PROCESS USING THE REACTOR

La présente invention prévoit un réacteur pour au moins deux matières liquides, comportant un logement de réacteur fermé (1) ; un tube d'alimentation (10) ayant des entrées de matière liquide (11, 12) destinées à recevoir des matières liquides correspondantes de manière respective ; un tube de distribution (20) qui communique avec le tube d'alimentation et s'étendant dans le logement de réacteur, le tube de distribution étant pourvu d'une pluralité de trous de distribution (21) dans la zone s'étendant dans le logement de réacteur ; un lit rotatif (30) sous la forme d'un cylindre creux, qui est disposé dans le logement de réacteur par l'intermédiaire d'un mécanisme de fixation (40), en divisant ainsi une cavité intérieure du logement de réacteur en une zone centrale (45) et une zone extérieure (46), le lit rotatif étant capable d'être entraîné en rotation par un mécanisme d'entraînement (42) ; et une sortie de matière (6) prévue dans une partie inférieure du logement de réacteur pour une ...

Catalyst for the alkylation of paraffinic hydrocarbons

Catalyseur à base d'un support poreux minéral ou organique et du mélange constitué par l'acide sulfurique, l'acide phosphorique et l'eau, son mode de préparation et son utilisation en alkylation catalytique d'isobutane et/ou d'isopentane en présence d'au moins une oléfine comportant de 3 à 6 atomes de carbone par molécule.

MEANS AND METHOD FOR CONTROLLING THE STRENGTH OF ACID IN AN ALKYLATION UNIT

LIQUID CATALYST Of ALIPHATIC ALKYLATION

L'invention concerne l'utilisation en alkylation catalytique d'au moins une isoparaffine choisie dans le groupe formé par l'isobutane et l'isopentane en présence d'au moins une oléfine comportant de 3 à 6 atomes de carbone par molécule d'un catalyseur comprenant de l'acide choisi parmi les acides de formule R-SO3 H, où R est le fluor ou un groupement alkyl ou un groupement alkyl fluoré, R étant de préférence F ou CF3 , de façon encore plus préférée CF3 , et un solvant aprotique organique faiblement basique.

Catalyst of isoparaffin C4-C5 alkylation by at least an olefin C2-C6

La présente invention concerne un catalyseur comprenant un support poreux organique ou minéral, de préférence de la silice, et une phase acide comportant le composé B(OSO2 CF3 )3 et au moins un acide choisi dans le groupe formé par l'acide sulfurique (H2 SO4 ) et l'acide trifluorométhanesulfonique (CF3 SO3 H), ledit support ayant été imprégné par ladite phase acide, ledit catalyseur étant tel qu'il est constitué essentiellement de particules de diamètre moyen compris entre 0,1 et 30 mum, ledit catalyseur étant caractérisé en ce que ladite phase acide comprend: - entre 0,1 et 70 % poids de composé B(OSO2 CF3 )3 ; - entre 0 et 90 % poids de H2 SO4 ; - entre 0 et 90 % poids de CF3 SO3 H. L'invention concerne aussi la préparation et l'utilisation dudit catalyseur en alkylation catalytique d'isobutane et/ou d'isopentane en présence d'au moins une oléfine comportant de 2 à 6 atomes de carbone par molécule, de préférence 3 à 6 atomes de carbone par molécule.

PROCESS Of ISOPARAFFIN C4-C5 ALKYLATION BY AT LEAST an OLEFIN C3-C6 IN BIPHASIC MEDIUM

L'invention concerne l'utilisation en alkylation catalytique d'au moins une isoparaffine choisie dans le groupe formé par l'isobutane et l'isopentane en présence d'au moins une oléfine comportant de 3 à 6 atomes de carbone par molécule d'un catalyseur constitué essentiellement d'acide sulfurique et du composé HB(HSO4 )4 , ledit catalyseur comprenant (en % poids) entre 0,4% et 68,8% du composé HB(HSO4 )4 et entre 31,2% et 99,6% du composé H2 SO4 , et ledit catalyseur ne contenant pas d'anhydride sulfurique.

Alkylation Process

Process of alkylation of an isoparaffin with an olefin

PROCESS FOR PARAFFIN-OLEFIN ALKYLATION

EQUIPMENT AND MODE OF REGULATION ALLOWING TO OBTAIN OPTIMAL OPERATING CONDITIONS Of an INSTALLATION,

PROCESS OF alquilacaoALQUILACAO WITH THE PRESENCE OF A CATALYSER I STRONG ELIMINATE ACID, CATALYTIC OF alquilacaoALQUILACAO AND PROCESS FOR ITS MANUFACTURE

ALKYLATION PROCESS WITH RECONTACTING IN SETTLER

A system and/or process for decreasing the level of at least one organic fluoride present in a hydrocarbon phase contained in an alkylation settler by contacting the hydrocarbon phase with an HF containing stream, containing greater than about 80 wt.% and less than about 94 wt. % HF, in the intermediate portion of the settler which contains at least one tray system, with each tray system comprising a perforated tray defining a plurality of perforations and a layer of packing below the perforated tray, are disclosed.

SYSTEM AND PROCESS FOR ALKYLATION

A method for alkylating a hydrocarbon comprising at least one isoparaffin and at least one olefin by introducing liquid acid catalyst and the hydrocarbon into a high shear reactor, forming an emulsion comprising droplets comprising hydrocarbon in a continuous acid phase, wherein the droplets have a mean diameter of less than about 5 microns, introducing the emulsion into a vessel operating under suitable alkylation conditions whereby at least a portion of the isoparaffin is alkylated with the olefin to form alkylate, and removing a product stream comprising alkylate from the vessel. A system for carrying out the method is also disclosed.

ACID CATALYST AND USE THEREOF IN ALKYLATION OF OLEFINS WITH TERTIARY ALKANES

The present invention provides an acid catalyst complex comprising an organosulfonic acid having at least one covalent carbon-fluorine bond or one covalent carbon-phosphorus bond provided by a phosphono radical which has been contacted with a Lewis Acid to produce a catalyst complex containing said Lewis Acid. The present invention also provides a process for the conversion of a reactant into a reaction product in the presence of said catalyst complex. In particular, the catalyst complex is useful for providing a high octane alkylate stream by converting a mixture comprising isoparaffins and olefins into said alkylate in the presence of said catalyst complex.

NOVEL REACTOR FOR IONIC LIQUID CATALYZED ALKYLATION BASED ON MOTIONLESS MIXER

Systems and apparatus for ionic liquid catalyzed hydrocarbon conversion may comprise a modular reactor comprising a plurality of mixer modules. The mixer modules may be arranged in series. One or more feed modules may be disposed between the mixer modules. Such systems may be used for ionic liquid catalyzed alkylation reactions. Processes for ionic liquid catalyzed hydrocarbon conversion are also disclosed. 1. A system for ionic liquid catalyzed hydrocarbon conversion , the system comprising:a modular reactor comprising a plurality of static mixer modules and one or more feed modules, wherein:said static mixer modules are arranged in series,each said static mixer module and each said feed module is vertically aligned,said static mixer modules are arranged alternately with said feed modules such that each feed module is disposed between two of said static mixer modules, andeach said static mixer module is arranged coaxially with each said feed module.2. The system according to claim 1 , wherein the number of said static mixer modules is n claim 1 , and the number of said feed modules is (n−1).3. The system according to claim 2 , wherein the number of said static mixer modules claim 2 , n claim 2 , is in the range from two (2) to 10.4. The system according to claim 1 , wherein:each said static mixer module is in contact with at least one of said feed modules, andeach said feed module is in contact with two of said static mixer modules.5. The system according to claim 1 , wherein:each said static mixer module and each said feed module has a circular cross-section, andeach said static mixer module and each said feed module has the same internal diameter.6. The system according to claim 1 , wherein each said static mixer module occupies essentially the entire cross-sectional area of the modular reactor.7. The system according to claim 1 , further comprising a feed supply line claim 1 , wherein:each said feed module includes a feed conduit,each said feed conduit is in ...

NOZZLE DESIGN FOR IONIC LIQUID CATALYZED ALKYLATION

Systems for ionic liquid catalyzed hydrocarbon conversion comprise a reactor vessel, a mixing device in fluid communication with the reactor vessel, and at least one circulation loop in fluid communication with the reactor vessel and the mixing device. The mixing device may comprise an upper venturi, at least one feed injection component, and a lower venturi. Such systems may be used for ionic liquid catalyzed alkylation reactions. Processes for ionic liquid catalyzed hydrocarbon conversion are also disclosed. 1. A system for ionic liquid catalyzed hydrocarbon conversion , the system comprising:a reactor vessel having a top; anda mixing device disposed at the top of the reactor vessel, wherein the mixing device comprises:an upper venturi having an axial outlet at the upper venturi distal end, the upper venturi distal end disposed within the reactor vessel,at least one feed injection array disposed within the reactor vessel, each said feed injection array coaxial with the upper venturi, anda lower venturi having an axial inlet at the lower venturi proximal end, the lower venturi proximal end disposed within the reactor vessel, wherein:the lower venturi inlet is spaced radially outward from the upper venturi outlet to define an inter-venturi channel between the upper venturi distal end and the lower venturi proximal end,the lower venturi is coaxial with the upper venturi,the mixing device is configured for projecting a central jet of a first liquid downward from the upper venturi outlet into the lower venturi, andeach said feed injection array is configured for projecting a second liquid toward an axis of the upper venturi.2. (canceled)3. The system according to claim 1 , wherein the lower venturi inlet is disposed at the same elevation or about the same elevation as the upper venturi outlet.4. The system according to claim 1 , wherein:the lower venturi has a lower venturi constriction point,the at least one feed injection array comprises a single feed injection array ...

INTEGRATION OF A DEHYDROGENATION UNIT AND AN ALKYLATION UNIT

The present invention relates to the integration of an alkylation unit for use in a hydrocarbon conversion process. More specifically, the present invention relates to the integration of a dehydrogenation unit and an alkylation unit and the placement of different isomerization units located off the deisobutanizer and the debutanizer. 1. A process for dehydrogenation and alkylation , comprising:passing a hydrocarbon stream to a dehydrogenation unit to generate a process stream comprising olefins;passing the process stream to a selective hydrogenation unit to generate a selective hydrogenation unit product stream;passing the selective hydrogenation unit product stream to a dehydrogenation fractionation unit to generate a light stream, a heavies stream, and a dehydrogenation fractionation product stream;passing the dehydrogenation fractionation product stream to an alkylation unit to produce an alkylation unit product stream;passing the alkylation unit product stream to a deisobutanizer to generate a deisobutanizer overhead stream and a deisobutanizer bottoms stream;passing the deisobutanizer bottoms stream to a debutanizer to generate a debutanizer overhead stream and a debutanizer products stream;passing a portion of the debutanizer overhead stream to an isomerization unit to generate an isomerization unit product stream which is passed to the deisobutanizer; andpassing a portion of the debutanizer overhead stream to the dehydrogenation unit.2. The process of claim 1 , further comprising passing a portion of the debutanizer overhead stream to an isomerization unit to generate an isomerization unit product stream which is passed to the deisobutanizer and passing a portion of the debutanizer overhead stream to the dehydrogenation unit.3. The process of claim 1 , further comprising passing a deisobutanizer side cut to an isomerization unit to generate an isomerization unit product stream which is passed to the deisobutanizer.4. The process of claim 1 , wherein the ...

Reactor and Alkylation Process Using the Reactor

The present disclosure provides a reactor for at least two liquid materials, comprising an enclosed reactor housing; a feeding tube having liquid material inlets for receiving corresponding liquid materials respectively; a distribution tube communicating with the feeding tube and extending into the reactor housing, the distribution tube being provided with a plurality of distribution holes in the region thereof extending into the reactor housing; a rotating bed in form of a hollow cylinder, which is disposed in the reactor housing via a fixing mechanism, thus dividing inner cavity of the reactor housing into a central area and an outer area, the rotating bed being capable of rotating driven by a driving mechanism; and a material outlet provided in a lower portion of the reactor housing for outputting product after reaction. The distribution tube extends into the central area spaced from inner surface of the rotating bed, so that materials can enter into the outer area from the central area through the rotating bed and can be output via the material outlet. 1. A reactor for at least two liquid materials , comprising ,an enclosed reactor housing;a feeding tube having liquid material inlets for receiving corresponding liquid materials respectively;a distribution tube communicating with the feeding tube and extending into the reactor housing, the distribution tube being provided with a plurality of distribution holes in the region thereof extending into the reactor housing;a rotating bed in form of a hollow cylinder, which is disposed in the reactor housing via a fixing mechanism, thus dividing inner cavity of the reactor housing into a central area and an outer area, the rotating bed being capable of rotating driven by a driving mechanism; anda material outlet provided in a lower portion of the reactor housing for outputting product after reaction,wherein the distribution tube extends into the central area spaced from inner surface of the rotating bed, so that ...

ALKYLATE BASE OIL OF BIOLOGICAL ORIGIN

An alkylate base oil of a biological origin having a kinematic viscosity at 100° C. from 3 mm/s to 20 mm/s, and characterized by having a total integral of a C NMR spectrum wherein 25-60% of the total integral of the C NMR spectrum falls within C NMR resonances in ranges for linear long chain alkyl groups given by: C1(13.9-14.2 ppm), C2(22.6-22.8 ppm), C3(31.9-32.05 ppm), C4(29.35-29.45 ppm), and C5+(29.6-29.8 ppm). 1. An alkylate base oil of a biological origin having a kinematic viscosity at 100° C. from 3 mm/s to 20 mm/s , and characterized by having a total integral of a C NMR spectrum wherein 25-60% of the total integral of the C NMR spectrum falls within C NMR resonances in ranges for linear long chain alkyl groups given by: C1(13.9-14.2 ppm) , C2(22.6-22.8 ppm) , C3(31.9-32.05 ppm) , C4(29.35-29.45 ppm) , and C5+(29.6-29.8 ppm).2. The alkylate base oil of claim 1 , additionally having a viscosity index of 50 to 140.3. The alkylate base oil of claim 1 , additionally having a viscosity index of 80 or greater.4. The alkylate base oil of claim 1 , wherein the alkylate base oil is saturated.5. The alkylate base oil of claim 1 , additionally having a bromine index less than 500 mg Br/100 g.6. The alkylate base oil of claim 5 , wherein the bromine index is less than 100 mg Br/100 g.7. The alkylate base oil of claim 1 , additionally having a long straight backbone with two long chain alkyl ends.8. The alkylate base oil of claim 1 , additionally having a pour point less than −15° C.9. The alkylate base oil of claim 1 , additionally having a cloud point less than −20° C.10. The alkylate base oil of claim 1 , wherein the biological origin is at least 95%.11. The alkylate base oil of claim 1 , wherein the alkylate base oil of the biological origin is an alkylation product of a farnesane that was made from a biologically derived feedstock.12. A finished lubricant claim 1 , comprising: the alkylate base oil of and at least one additive selected from the group consisting of ...

REVERSE ACID AND HYDROCARBON CASCADING IN ALKYLATION

A cascade reactor scheme with acid and hydrocarbon flowing in reverse directions. The systems and processes for alkylation of olefins herein may include providing a first olefin to a first alkylation zone, and a second olefin to a second alkylation zone. Isoparaffin may be provided to the first alkylation zone. The isoparaffin and first olefin may be contacted with a partially spent sulfuric acid in the first alkylation zone to form a spent acid phase and a first hydrocarbon phase including alkylate and unreacted isoparaffin. The first hydrocarbon phase and second olefin may be contacted with a sulfuric acid feed in the second alkylation zone to form a second hydrocarbon phase, also including alkylate and unreacted isoparaffin, and the partially spent sulfuric acid that is fed to the first alkylation zone. Further, the second hydrocarbon phase may be separated, recovering an isoparaffin fraction and an alkylate product fraction. 1. A system for the alkylation of olefins , the system comprising:a first flow line for providing a first olefin to a first alkylation zone;a second flow line for providing a second olefin to a second alkylation zone, wherein the second olefin may be the same or different than the first olefin;a third flow line for providing an isoparaffin to the first alkylation zone;the first alkylation zone, for contacting the isoparaffin and the first olefin with a partially spent sulfuric acid under alkylation conditions to form a spent acid phase and a first hydrocarbon phase comprising alkylate and unreacted isoparaffin;the second alkylation zone for contacting the first hydrocarbon phase and the second olefin with a fresh sulfuric acid feed under alkylation conditions to form a second hydrocarbon phase, comprising alkylate and unreacted isoparaffin, and the partially spent sulfuric acid fed to the first alkylation zone; anda separator for separating the second hydrocarbon phase to recover an isoparaffin fraction and an alkylate product fraction.2. ...

COST-EFFECTIVE MATERIALS FOR PROCESS UNITS USING ACIDIC IONIC LIQUIDS

We provide an apparatus for performing a hydrocarbon conversion or for handling of an output of the hydrocarbon conversion, comprising: a bare metal alloy, wherein the bare metal alloy comprises: from 15.1 to 49 wt % nickel, from 2.3 to 10 wt % molybdenum, from 0.00 to 2.95 wt % copper, and 20 to 59 wt % iron; wherein the bare metal alloy exhibits a corrosion rate less than 0.07 mm/year when performing the hydrocarbon conversion or handling the output of the hydrocarbon conversion; and wherein the hydrocarbon conversion is performed using an acidic ionic liquid. We also provide a process for using the apparatus. 1. An apparatus configured for performing a hydrocarbon conversion using an acidic ionic liquid that comprises a metal halide , or for handling of an output of the hydrocarbon conversion , comprising: a bare metal alloy , wherein the bare metal alloy comprises:from 15.1 to 49 wt % nickel, from 2.3 to 10 wt % molybdenum, from 0.00 to 2.95 wt % copper, and 20 to 59 wt % iron; andwherein the bare metal alloy exhibits a corrosion rate less than 0.07 mm/year when performing the hydrocarbon conversion or handling the output of the hydrocarbon conversion.2. The apparatus of claim 1 , wherein the bare metal alloy is an austenitic stainless steel.3. The apparatus of claim 1 , wherein the bare metal alloy comprises at least 35 wt % nickel and has resistance to chloride stress corrosion cracking.4. The apparatus of claim 1 , wherein the apparatus is selected from the group consisting of a reactor claim 1 , a conduit claim 1 , a fitting claim 1 , a heat exchanger claim 1 , a phase separator claim 1 , a distillation unit claim 1 , and combinations thereof.5. The apparatus of claim 1 , wherein the apparatus is configured to produce an alkylate gasoline blending component claim 1 , a distillate fuel claim 1 , a base oil claim 1 , or combinations thereof.6. The apparatus of claim 1 , wherein the apparatus is manufactured or adapted to comprise at least 70 wt % of the bare ...

Process of Alkylation of Isobutane with Olefins

The process for producing an alkylate is intended for use in the oil refining and hydrocarbon process industry. The process comprises reacting isobutane with an alkylation agent (an olefin) in the presence of a solid acidic catalyst and a C4+ solvent. Thus, a system is obtained, wherein the solid acidic catalyst is suspended in a solvent and the suspension is maintained by passing the feed stream through the catalyst-solvent system, thereby providing a uniform catalyst distribution throughout the entire volume and enabling the reaction to be carried out at low pressures. 1. A process for producing an alkylate by reacting isobutane with an olefin in the presence of a solid acidic catalyst in a suspension , the process comprising:suspending the solid acidic catalyst in a C4+ hydrocarbon solvent;supplying a feed stream in an amount sufficient to maintain the suspension in a stable state, wherein the feed stream comprises isobutane and olefin, and wherein a boiling point of the C4+ hydrocarbon solvent is higher than a boiling point of a lowest boiling point hydrocarbon of the feed stream; andcarrying out the process at a temperature above the boiling point of the lowest boiling point hydrocarbon of the feed stream, but below the boiling point of the C4+ hydrocarbon solvent.2. The process of claim 1 , wherein the solid acidic catalyst has a particle size of about 20-500 μm.3. The process of claim 1 , wherein the solid acidic catalyst is selected from promoted or non-promoted Y and/or BEA type zeolites or solid superacids.4. The process of claim 3 , wherein a solid superacid of the solid superacids is selected from sulfated zirconium oxide and/or tungsten zirconium oxide.5. The process of claim 1 , wherein a molar ratio of the isobutene to olefin in the feed stream is from about 10:1 to about 500:1.6. The process of claim 1 , wherein the C4+ hydrocarbon solvent comprises an n-paraffin and/or an alkylate.7. The process of claim 6 , wherein said n-paraffin is selected from ...

ALKYLATION PROCESS WITH THERMAL OXIDATION SYSTEM

Processes for treating effluent streams in alkylation processes are described. One or more process streams rom HF alkylation processes, HSOalkylation processes, or ionic liquid alkylation processes can be thermally oxidized in a thermal oxidation system. The thermal oxidation system can replace at least one of the caustic wash unit, the neutralization unit, and the acid gas treatment unit. 1. A process for treating off-gas and waste effluent streams in an alkylation complex comprising:{'claim-text': {'sub': ['2', '2', '2', '2', '2', '2', '2', '2', '3', '2', '4', '2', '3', '2', '3', '4', '3', '2', '2', '2', '3', '2', '4', '2', '3', '2', '3', '2', '2', '3', '3', '4'], '#text': 'thermally oxidizing the at least one of: the acid ASO stream from the liquid acid alkylation process section, the acid gas stream from the liquid acid alkylation process section, the acid liquid stream from the liquid acid alkylation process section, the acid spent ionic liquid from the ionic liquid alkylation process section, the acid gas stream from the ionic liquid alkylation process section, the neutralized ASO stream from the caustic wash zone, and the spent caustic stream from the acid gas scrubber zone; or the acid liquid stream from the ionic liquid alkylation process section, the neutralized spent ionic liquid from the ionic liquid caustic wash zone, and the spent caustic stream from the acid gas scrubber zone, in a thermal oxidizing section forming flue gas consisting essentially of at least one of HO, CO, N, O, SOx, NOx, HCl, Cl, HF, F, NaO, NaSO, NaSO, NaCO, NaCl, NaF, CaF, CaO, CaSO, CaSO, CaCO, CaCl, KO, KSO, KSO, KCO, KCl, KF, AlO, NiO, FeO, FeO, FeO, FeO, and CuO;'}, '#text': 'thermally oxidizing at least one of: an acid soluble oil (acid ASO) stream from a liquid acid alkylation process section, an acid gas stream from the liquid acid alkylation process section, an acid liquid stream from the liquid acid alkylation process section, a neutralized ASO stream from a caustic wash ...

COMPOSITION OF ISOALKANE ALKYLATE BASE OIL

An isoalkane alkylate base oil consisting predominantly of long carbon chain molecules having a straight chain of no less than 12 carbons and having at least one branch towards the middle of the straight chain, and characterized by: 1. An isoalkane alkylate base oil that is essentially free of olefins and aromatics and consists predominantly of long carbon chain molecules having a straight chain of no less than 12 carbon atoms and having at least one branch towards the middle of the straight chain , and characterized by:a) the isoalkane alkylate base oil contains less than 10 wt % n-alkanes, less than 0.1 wt % olefinic hydrocarbons, and less than 0.1 wt % aromatic hydrocarbons;b) the at least one branch is a branched alkyl group containing 4 or more carbon atoms; andc) the long carbon chain molecules have two terminal linear unbranched alkyl groups each containing at least 4 carbons.2. An isoalkane alkylate base oil , characterized by having a total integral of the C NMR spectrum wherein more than 25% of the total integral of the C NMR spectrum falls within C NMR resonances in ranges for linear long chain alkyl groups given by: C1(13.9-14.2 ppm) , C2(22.6-22.8 ppm) , C3(31.9-32.05 ppm) , C4(29.35-29.45 ppm) , and C5+(29.6-29.8 ppm).3. The isoalkane alkylate base oil of claim 2 , wherein more than 50% of the total integral of the C NMR spectrum falls within the C NMR resonances in the ranges for linear long chain alkyl groups.4. The isoalkane alkylate base oil of claim 2 , wherein the isoalkane alkylate base oil has a viscosity index greater than 90 and the total integral of the C NMR spectrum falling with the C NMR resonances in the ranges for linear long chain alkyl groups is from 26% to 80%.5. The isoalkane alkylate base oil of or claim 2 , wherein the isoalkane alkylate base oil has a viscosity index from 91 to 200.6. The isoalkane alkylate base oil of or claim 2 , wherein the isoalkane alkylate base oil has a bromine index less than 2000 mg Br/100 g.7. The ...

SULFURIC ACID ALKYLATION REACTOR SYSTEM AND CONVERSION OF A HYDROGEN FLUORIDE ALKYLATION UNIT TO A SULFURIC ACID ALKYLATION UNIT

This disclosure relates to SA alkylation reactor systems. The reactor system involves a closed reactor vessel comprising a shell, a vapor outlet, and an emulsion outlet. The reactor system also involves a distributor located at the lower portion of the reactor vessel, a mixer fluidly connected with the distributor, and an emulsion pump fluidly connected with the mixer and the emulsion outlet, wherein the emulsion pump is located outside the reactor vessel. This disclosure also relates to a split SA alkylation reactor system wherein a single horizontal reactor vessel is divided to accommodate two reactor systems. This disclosure also relates to alkylation processes using the reactor systems. This disclosure also relates to methods of converting an HF alkylation unit to a SA alkylation unit. This disclosure also relates to converted SA alkylation units and alkylation processes performed in the converted SA alkylation units. 1. A sulfuric acid alkylation reactor system comprising:(a) a closed reactor vessel comprising a shell, a vapor outlet, and an emulsion outlet;(b) a distributor located at the lower portion of the reactor vessel;(c) a mixer fluidly connected with the distributor; and(d) an emulsion pump fluidly connected with the mixer and the emulsion outlet;wherein the emulsion pump is located outside the reactor vessel.2. The sulfuric acid alkylation reactor system of claim 1 , wherein the mixer is an internal static mixer located at the lower portion of the reactor vessel claim 1 , the distributor is downstream of the internal static mixer and is directly connected with the internal static mixer.3. The sulfuric acid alkylation reactor system of further comprising an external static mixer fluidly connected with the internal static mixer and the emulsion pump claim 2 , wherein the external static mixer is located outside the reactor vessel.4. The sulfuric acid alkylation reactor system of claim 1 , wherein the mixer is an in-line rotor stator mixer fluidly ...

CONTINUOUS MIXING REACTOR AND METHOD OF USE

A continuous mixing reactor has an outer shell having a cylindrical portion with a central section and two opposite conical end sections; a circulation tube within the shell so that an annular passage forms between the shell and the circulation tube; an impeller within and positioned adjacent to one end of the circulation tube; and heat exchange means penetrating the outer shell and extending into the end of the circulation tube opposite the impeller. The outer shell has a hydraulic head forming one end of the shell, a heat exchange medium header at the opposite end of the shell. The circulation tube nearer the heat exchange medium header terminates at or downstream from a tangential plane extending through the shell at the intersection of the central section and the conical end section of the cylindrical portion of shell. The reactor is useful in an alkylation process. 1. A continuous mixing reactor having (a) an outer shell , wherein the outer shell has an interior wall and an exterior wall; one or more inlets for fluids , a hydraulic head (or circulating head) forming one end of the shell , a heat exchange medium header at the opposite end of the shell from the hydraulic head; wherein the shell has a generally cylindrical portion between the hydraulic head and the heat exchange medium header , having a central section and two opposite end sections , the central section having a substantially uniform diameter and each end section is a conical section , and a discharge outlet positioned on a surface of the cylindrical portion; and (b) a hollow circulation tube , open at both ends , extending from the hydraulic head to a terminal end opposite of the hydraulic head and nearer to the heat exchange medium header , and positioned axially within the shell and spaced from the interior wall thereof such that an annular passage is formed between the circulation tube and the shell; and (c) an impeller received within and positioned adjacent to the end of the circulation tube ...

DIVIDING WALL COLUMN IN ALKYLATION PROCESS FOR REACTOR RECYCLE AND PRODUCT SEPARATION

A dividing wall column is used in an alkylation process flow scheme to fractionate an alkylate reactor effluent to produce an iso-butane-rich stream as a recycle feed for the alkylation reactor while also separating iso-butane, normal butane and alkylate as separate product streams depending on the reactor effluent composition. In an optional embodiment, the scheme may contain propane. 54422610. The alkylation system of claim where the overhead iso-butane-rich stream () is a recycle stream () to the alkylation reaction/regeneration section ().6422146016. The alkylation system of claim where the alkylate product stream () is routed to a battery limit after preheating the alkylate reactor effluent () in a heat exchanger () prior to being fed to the DWC ().74485032. The alkylation system of claim further comprising an intermediate reboiler () in a bottom section () of the DWC ().8464830. The alkylation system of where the alkylate product () is a heating medium in the intermediate reboiler () before it preheats the alkylate reactor effluent ().942428241210. The alkylation system of claim where the make-up iso-butane () is at least a portion of the iso-butane product () and the make-up iso-butane () is routed to the olefin feed () upstream of the alkylation reaction/regeneration section () to form a mixture.1010. The alkylation system of in the absence of a fractionation section of the alkylation reaction/regeneration section () claim 9 , configured to fractionating the mixture.11123. The alkylation system of any one of claim claim 9 , claim 9 , or where:{'b': 30', '34', '32, 'the alkylate reactor effluent () containing propane is a feed to a pre-fractionator section () of the DWC ();'}{'b': 32', '53', '54, 'the DWC () has an overhead product () containing propane routed to a depropanizer column ();'}{'b': 32', '56', '36', '32', '26', '10, 'the DWC () has an iso-butane-rich stream that is the iso-butane product stream is a first side draw product (), taken from a main- ...

IONIC LIQUID REACTOR WITH HEAT EXCHANGER

An ionic liquid reactor unit and a process for controlling heat generation from an ionic liquid reactor unit. The ionic liquid reactor unit may include an external heat exchanger. The effluent from the reactor is separated in a separation zone allowing the hydrocarbon phase to transfer heat to a cooling fluid. The heat exchanger may be a tube-in-shell, a spiral plate heat exchanger, a hair pin heat exchanger. The heat exchanger accommodates the separation of the ionic liquid from the hydrocarbon phase, and may allow for the ion liquid to be drained. 1. An ionic liquid catalyst reactor unit comprising:a first reaction zone having an inlet for ionic liquid, an inlet for a hydrocarbon stream, and an outlet for an effluent stream;a separation zone configured to receive the effluent stream and separate the effluent stream into a hydrocarbon phase and an ionic liquid phase; and,a first heat exchange zone configured to receive at least a portion of the effluent stream from the first reaction zone and comprising: an outlet for a cooled effluent stream, and an outlet for ionic liquid.2. The ionic liquid catalyst reactor unit of wherein the first heat exchange zone comprises a heat exchanger with a shell and wherein the separation zone is disposed within the shell.3. The ionic liquid catalyst reactor unit of wherein the shell includes an inlet for the effluent stream disposed below the outlet for the cooled effluent stream.4. The ionic liquid catalyst reactor unit of claim 1 , wherein the first heat exchange zone comprises a heat exchanger comprising a shell and at least one baffle in the shell.5. The ionic liquid catalyst reactor unit of wherein the at least one baffle comprises a baffle selected from the group consisting of: a helical baffle; a rod baffle; a grid baffle; an expanded metal baffle; and claim 4 , a segmental baffle.6. The ionic liquid catalyst reactor unit of wherein the heat exchanger is configured to receive the effluent stream in a direction countercurrent ...

INTEGRATED PROCESS FOR NORMAL PARAFFIN ALKYLATION

An integrated alkylation and disproportionation process and apparatus are described. n-Cand n-Care routed to a disproportionation reaction zone for conversion to iso-Cand C isoparaffin-rich product. The iso-Cis routed to an alkylation reaction zone and reacted with refinery propylene and butenes to produce alkylate product. The C isoparaffin-rich product and alkylate product are recovered. Unconverted iso-Cand/or olefins are recycled to the alkylation reaction zone, and unconverted n-Cand n-Care recycled to the disproportionation reaction zone. 1. A process for normal paraffin alkylation comprising:{'sub': 4', '5', '4', '6+', '4', '5, 'introducing a feed comprising n-Cand n-Cparaffins to a disproportionation reaction zone in the presence of a disproportionation catalyst under disproportionation reaction conditions to form a disproportionation mixture comprising iso-Cand C disproportionation products and unreacted n-Cand n-Cparaffins;'}{'sub': 4', '6+', '4', '5, 'separating the disproportionation mixture in a disproportionation separation zone into at least an iso-C-rich stream, a C isoparaffin-rich stream, and a stream rich in unreacted n-Cand n-Cparaffins;'}{'sub': 4', '4, 'introducing the iso-C-rich stream and an olefin feed stream comprising at least one of ethylene, propylene, and butenes into an alkylation reaction zone in the presence of an alkylation catalyst under alkylation reaction conditions to produce an alkylation mixture comprising alkylate and unreacted iso-Cparaffins;'}{'sub': '4', 'separating the alkylation mixture in an alkylation separation zone into at least an alkylate-rich stream, and a stream rich in unreacted iso-Cparaffins;'}{'sub': 4', '5, 'recycling the stream rich in unreacted n-Cand n-Cparaffins from the disproportionation separation zone to the disproportionation reaction zone;'}{'sub': '4', 'recycling the stream rich in unreacted iso-Cparaffins from the alkylation separation zone to the alkylation reaction zone; and'}{'sub': '6+', ' ...

INTEGRATED PROCESS FOR GASOLINE PRODUCTION

An integrated process for gasoline production is described. The process includes introducing a feed comprising n-Chydrocarbons into a disproportionation reaction zone in the presence of a disproportionation catalyst to form a disproportionation mixture comprising iso-Cand Cdisproportionation products and unreacted n-Chydrocarbons. An iso-Chydrocarbon stream and an olefin feed are introduced into an alkylation reaction zone in the presence of an alkylation catalyst to produce an alkylation mixture comprising alkylate and unreacted iso-Cparaffins. The disproportionation mixture and the alkylation mixture are combined, and the combined mixture is separated into at least a stream comprising the alkylate product, an iso-Cstream, and an unreacted n-Chydrocarbon stream. The iso-Cstream is recycled to the alkylation reaction zone, and the unreacted n-Chydrocarbon stream is recycled to the disproportionation reaction zone. The stream comprising the alkylate product is recovered. 1. An integrated process for gasoline production comprising:{'sub': 5', '4', '6+', '5, 'introducing a feed comprising n-Chydrocarbons to a disproportionation reaction zone in the presence of a disproportionation catalyst under disproportionation reaction conditions to form a disproportionation mixture comprising iso-Cand Cdisproportionation products and unreacted n-Chydrocarbons;'}{'sub': 4', '4, 'introducing an iso-Chydrocarbon stream and an olefin feed stream comprising at least one of ethylene, propylene, and butenes into an alkylation reaction zone in the presence of an alkylation catalyst under alkylation reaction conditions to produce an alkylation mixture comprising alkylate product and unreacted iso-Cparaffins;'}combining the disproportionation mixture and the alkylation mixture to form a combined mixture;{'sub': 4', '4', '4,', '5, 'separating the combined mixture into at least a stream comprising the alkylate product, an iso-Cstream comprising the iso-Cdisproportionation product and the ...

PRODUCTION OF ALKYLATE FROM LIGHT ALKANES

Systems and methods are provided for forming alkylate from an isoparaffin-containing feed. Olefins for the alkylation reaction can be generated from a portion of the isoparaffin-containing feed. This can be achieved, for example, by using selective oxidation to convert a portion of isoparaffins into alcohol, such as conversion of isobutane to t-butyl alcohol. The alcohol can then be converted to an alkene, such as conversion of t-butyl alcohol to isobutene, in the alkylation reaction environment in the presence of a solid acid catalyst. The solid acid catalyst can then facilitate alkylation of isoparaffin using the in-situ formed alkenes. A catalyst having an MWW framework is an example of a suitable solid acid catalyst. 1. A method for producing alkylate , comprising:exposing an isoparaffin-containing feed to oxidation conditions in the presence of oxygen to form an oxidation effluent comprising tertiary alcohol, at least 0.5 wt % of the isoparaffins in the isoparaffin-containing feed being converted under the oxidation conditions;exposing at least a portion of the oxidation effluent to a solid acid catalyst under alkylation conditions to form an alkylation effluent, the at least a portion of the oxidation effluent comprising a molar ratio of isoparaffin to tertiary alcohol of about 5:1 to about 200:1.2. The method of claim 1 , wherein the isoparaffin-containing feed comprises at least 80 wt % C isoparaffins relative to a weight of the isoparaffin-containing feed.3. The method of claim 1 , wherein the isoparaffin-containing feed comprises at least 80 wt % C-Cisoparaffins relative to a weight of the isoparaffin-containing feed.4. The method of claim 1 , wherein the isoparaffin-containing feed comprises at least 80 wt % isobutane relative to a weight of the isoparaffin-containing feed.5. The method of claim 1 , wherein the oxidation effluent comprises a molar ratio of isoparaffin to tertiary alcohol of about 10:1 to about 100:1 claim 1 , or wherein the at least a ...

PRODUCTION OF HIGH OCTANE HYDROCARBON FROM LIGHT ALKANE FEED USING OXIDATION AND ACID CATALYSIS CHEMISTRY

Systems and methods are provided for production of high octane hydrocarbon from an isoparaffin feed using oxidation acid catalysis chemistry. 1. A method for the production of high octane hydrocarbon , comprising:oxidizing an isobutane containing feed in the presence of oxygen to form an oxidation effluent comprising tert-butyl alcohol (“TBA”) and an oxygenate impurity, at least 0.5 wt % of the isobutane in the isobutane containing feed being converted under the oxidation conditions;{'sub': '4', 'exposing at least a portion of the oxidation effluent to a solid acid catalyst, wherein the solid acid catalyst comprises a crystalline microporous material of the MWW framework type, under dehydration conditions to form a dehydration effluent comprising Chydrocarbons; at least 80% of the TBA being converted under the dehydration conditions;'}{'sub': 8', '8', '8, 'exposing at least a portion of the dehydration effluent to a second solid acid catalyst, wherein the second solid acid catalyst comprises a crystalline microporous material of the MWW framework type, under dimerization conditions to form a dimerization effluent comprising Chydrocarbons, wherein at least 90% of the Chydrocarbons in the dimerization effluent are Colefins.'}2. The method of claim 1 , further comprising hydrogenating the Colefins.3. The method of claim 1 , further comprising converting an n-butane containing feed to isobutane via isomerization over a bifunctional catalyst to form the isobutane containing feed.4. The method of claim 1 , wherein the oxygenate impurity comprises water claim 1 , methanol claim 1 , acetone claim 1 , or a combination thereof.5. The method of claim 4 , wherein the oxygenate impurity comprises methanol and acetone.6. The method of claim 3 , further comprising:{'sub': '8', 'hydrogenating the Colefins; and'}recycling a portion of unconverted n-butane, unconverted isobutane, or a combination of unconverted n-butane and unconverted isobutane to the n-butane containing feed.7. The ...

PRODUCTION OF ISO-OCTENE FROM TERTIARY ALCOHOLS

Systems and methods are provided for forming alkylate from a tertiary alcohol feed. Olefins for the alkylation reaction can be generated from a portion of the tertiary alcohol feed. The tertiary alcohol feed can be obtained, for example, by selective oxidation to convert a portion of an isoparaffin-containing feed into alcohol, such as conversion of isobutane to t-butyl alcohol. The alcohol can then be converted to an alkene, such as conversion of t-butyl alcohol to isobutene, in the alkylation reaction environment in the presence of a solid acid catalyst. The solid acid catalyst can then facilitate dimerization of the alkenes (e.g. isobutene) to form C olefins (e.g. isooctene). A catalyst having an MWW framework is an example of a suitable solid acid catalyst. 1. A method for the production of iso-octene , comprising:exposing a tent-butyl alcohol (“TBA”) containing feed to a solid acid catalyst, wherein the solid acid catalyst comprises a crystalline microporous material of the MWW framework type, under dehydration conditions to convert a percentage of TBA to isobutene to form an isobutene containing feed;exposing at least a portion of the isobutene containing feed to a second solid acid catalyst, wherein the second solid acid catalyst comprises a crystalline microporous material of the MWW framework type, under dimerization conditions to dimerize isobutene molecules in the isobutene containing feed to iso-octene to form an iso-octene containing feed; wherein greater than 50% of the iso-octene molecules in the iso-octene containing feed comprise trimethylpentene relative to weight of the iso-octene feed.2. The method of claim 1 , wherein the crystalline microporous material of the MWW framework type of either the first or second solid acid catalyst is selected from the group consisting of MCM-22 claim 1 , PSH-3 claim 1 , SSZ-25 claim 1 , ERB-1 claim 1 , ITQ-1 claim 1 , ITQ-2 claim 1 , MCM-36 claim 1 , MCM-49 claim 1 , MCM-56 claim 1 , EMM-10 claim 1 , EMM-12 claim ...

METHODS AND SYSTEMS FOR CONVERTING HYDROCARBONS

Methods and systems for converting hydrocarbons including exposing a portion of a hydroperoxide-containing feed including tert-butyl hydroperoxide to a solid deperoxidation catalyst under decomposition conditions to form an oxidation effluent comprising tert-butyl alcohol, wherein the solid deperoxidation catalyst comprises a manganese oxide octahedral molecular sieve, are provided herein. Further methods and systems for converting the oxidation effluent to an alkylation product are also provided herein. 1. A method for converting hydrocarbons , comprising:an oxidizing step comprising exposing a portion of a hydroperoxide-containing feed comprising tert-butyl hydroperoxide to a solid deperoxidation catalyst under decomposition conditions to form an oxidation effluent comprising tert-butyl alcohol,wherein the solid deperoxidation catalyst comprises a manganese oxide octahedral molecular sieve.2. The method of claim 1 , wherein the decomposition conditions comprise a temperature of about 50° C. to about 170° C. and a pressure of about 10 psig to about 500 psig.3. The method of claim 1 , wherein at least about 70% of the tert-butyl hydroperoxide is converted to tert-butyl alcohol and/or the solid deperoxidation catalyst has a selectivity of at least about 70% for conversion of tert-butyl hydroperoxide to tert-butyl alcohol.4. The method of claim 1 , wherein at least about 90% of the tert-butyl hydroperoxide is converted to tert-butyl alcohol and/or the solid deperoxidation catalyst has a selectivity of at least about 90% for conversion of tert-butyl hydroperoxide to tert-butyl alcohol.5. The method of claim 1 , wherein the manganese oxide octahedral molecular sieve comprises MnOoctahedra which share edges to form a tunnel structure.6. The method of claim 5 , wherein the tunnel structure is 2×2 tunnel structure or 3×3 tunnel structure.7. The method of claim 1 , wherein the solid deperoxidation catalyst is selected from the group consisting of OMS-2 claim 1 , Nb-OMS-2 ...

APPARATUS FOR REGENERATION OF ACIDIC IONIC LIQUID WITHOUT ADDITION OF A HYDROGENATION CATALYST

We provide a process for regenerating a spent acidic ionic liquid, comprising contacting the spent acidic ionic liquid with hydrogen and without an addition of a hydrogenation catalyst; wherein a conjunct polymer content is decreased in the spent acidic ionic liquid to produce regenerated acidic ionic liquid. We also provide a process for making an alkylate gasoline blending component, comprising: a) alkylating a mixture of isoparaffins and olefins using an acidic ionic liquid and an alkyl halide or a hydrogen halide, wherein a conjunct polymer accumulates in a spent acidic ionic liquid; and b) feeding the spent acidic ionic liquid and a hydrogen, and without an addition of a hydrogenation catalyst, to a regeneration reactor operated under selected hydrogenation conditions to produce a regenerated acidic ionic liquid that is used for the alkylating, wherein the conjunct polymer in the regenerated acidic ionic liquid is decreased by at least 50 wt %. 1. An apparatus for regenerating a spent acidic ionic liquid , comprising a vessel comprising an inlet for introducing a hydrogen , a second inlet on the vessel for introducing the spent acidic ionic liquid , an equipment in the vessel that provides mixing of the hydrogen and the spent acidic ionic liquid , a vent on the vessel , no parts for separately adding a hydrogenation catalyst to the vessel , and an outlet on the vessel for removing a regenerated acidic ionic liquid; wherein the apparatus is used for performing a process for regenerating the spent acidic ionic liquid , the process comprising contacting the spent acidic ionic liquid in the vessel used for the contacting with the hydrogen and without an addition of the hydrogenation catalyst; wherein a content of a conjunct polymer is decreased in the spent acidic ionic liquid to produce the regenerated acidic ionic liquid.2. The apparatus of claim 1 , additionally comprising an internal particulate filter claim 1 , in the vessel claim 1 , having no hydrogenation ...

CONVERSION OF A HYDROGEN FLUORIDE ALKYLATION UNIT TO A SULFURIC ACID ALKYLATION UNIT AND APPARATUS UTILIZED THEREIN

This disclosure relates to methods of converting an HF alkylation unit which utilizes HF as a reaction catalyst to a sulfuric acid alkylation unit which utilizes sulfuric acid as a reaction catalyst. This disclosure also relates to a segmented sulfuric acid settler for separating a sulfuric acid phase from a hydrocarbon phase. This disclosure also relates to methods of converting a vertical HF acid settler to a segmented sulfuric acid settler. This disclosure also relates to converted sulfuric acid alkylation units and alkylation processes performed in the converted sulfuric acid alkylation units. 1. A method for converting a hydrogen fluoride alkylation unit which utilizes hydrogen fluoride as a reaction catalyst to a sulfuric acid alkylation unit , the hydrogen fluoride alkylation unit comprising an HF alkylation reactor , an HF alkylation fractionation section comprising at least one fractionator , and an HF acid relief neutralizer vessel , the method comprising:(a) substituting sulfuric acid for hydrogen fluoride as the reaction catalyst;(b) retaining the HF acid relief neutralizer vessel as a blowdown vapor scrubber;(c) retaining the HF alkylation fractionation section as a sulfuric acid alkylation fractionation section;(d) providing at least one sulfuric acid alkylation reactor;(e) providing a refrigeration section comprising a refrigerant compressor and a heat exchanger for condensing a vapor stream from the refrigerant compressor;(f) providing a conduit for recycling an isoparaffin comprising isobutane from the refrigeration section to said at least one sulfuric acid alkylation reactor; and(g) providing a feed/effluent heat exchanger for cooling a hydrocarbon feed stream and heating a net effluent stream.2. A segmented sulfuric acid settler for separating a sulfuric acid phase from a hydrocarbon phase , the sulfuric acid settler comprising:(a) a vertical vessel having an outlet at its top section, a vertical interior wall, and a bottom;(b) at least one ...

REGENERATION OF ACIDIC IONIC LIQUID WITHOUT ADDITION OF A HYDROGENATION CATALYST

We provide a process for regenerating a spent acidic ionic liquid, comprising contacting the spent acidic ionic liquid with hydrogen and without an addition of a hydrogenation catalyst; wherein a conjunct polymer content is decreased in the spent acidic ionic liquid to produce regenerated acidic ionic liquid. We also provide a process for making an alkylate gasoline blending component, comprising: a) alkylating a mixture of isoparaffins and olefins using an acidic ionic liquid and an alkyl halide or a hydrogen halide, wherein a conjunct polymer accumulates in a spent acidic ionic liquid; and b) feeding the spent acidic ionic liquid and a hydrogen, and without an addition of a hydrogenation catalyst, to a regeneration reactor operated under selected hydrogenation conditions to produce a regenerated acidic ionic liquid that is used for the alkylating, wherein the conjunct polymer in the regenerated acidic ionic liquid is decreased by at least 50 wt %. 1. A process for regenerating a spent acidic ionic liquid , comprising contacting the spent acidic ionic liquid with a hydrogen and without an addition of a hydrogenation catalyst; wherein a content of a conjunct polymer is decreased in the spent acidic ionic liquid to produce a regenerated acidic ionic liquid.2. The process of claim 1 , wherein the contacting occurs at a temperature from 100° C. to 350° C.3. The process of claim 1 , wherein the contacting occurs in a vessel with an agitation rate of 50 to 2500 rpm.4. The process of claim 1 , wherein the contacting occurs in a vessel under a pressure of 50 to 5000 psig (446 to 34600 kpa).5. The process of claim 1 , wherein a contacting time is from 2 to 50 hours.6. The process of claim 1 , wherein the spent acidic ionic liquid comprises greater than 3 wt % of the conjunct polymer.7. The process of claim 1 , wherein the regenerated acidic ionic liquid comprises less than 1.5 wt % of the conjunct polymer.8. The process of claim 1 , wherein the spent acidic ionic liquid ...

ALKYLATION WITH OLEFIN MIXTURES

This disclosure relates to alkylation processes. The process involves providing two or more reaction zones disposed in sequence. In at least the first two reaction zones, olefin mixture comprising C3 and C4 olefins is contacted with isoparaffin comprising isobutane in the presence of sulfuric acid solution under effective alkylation conditions to produce a product mixture comprising spent acid solution and alkylate product, wherein the molar ratio of C3 to C4 olefins in the olefin mixture decreases in each subsequent reaction zone. In the process, the sulfuric acid solution present in a reaction zone contains the spent acid solution produced in the immediately preceding reaction zone. 1. An alkylation process comprising:(a) providing three or more reaction zones disposed in sequence;(b) contacting a non-final olefin mixture comprising C3 and C4 olefins with an isoparaffin comprising isobutane in the presence of a non-final sulfuric acid solution under effective alkylation conditions in each non-final reaction zone to produce a product mixture comprising a non-final spent acid solution and an alkylate product; and(c) contacting a final olefin comprising an olefin selected from the group consisting of C4 olefins, C5 olefins and mixtures thereof with an isoparaffin comprising isobutane in the presence of a final sulfuric acid solution under effective alkylation conditions in a final reaction zone to produce a product mixture comprising a final spent acid solution and an alkylate product;wherein the molar ratio of C3 to C4 olefins in the non-final olefin mixture decreases in each subsequent non-final reaction zone, and the sulfuric acid solution present in a reaction zone comprises the spent acid solution produced in the immediately preceding reaction zone.2. The alkylation process of wherein the sulfuric acid solution present in a reaction zone between a first reaction zone and the final reaction zone further comprises an additional sulfuric acid solution having higher ...

INTEGRATION OF A DEHYDROGENATION UNIT AND AN ALKYLATION UNIT

The present invention relates to the integration of an alkylation unit for use in a hydrocarbon conversion process. More specifically, the present invention relates to the integration of a dehydrogenation unit and an alkylation unit and the placement of different isomerization units located off the deisobutanizer and the debutanizer. 1. A process for dehydrogenation and alkylation , comprising:passing a field butane stream comprising isobutane and n-butane directly to a dehydrogenation unit to generate a stream comprising isobutane, isobutene, n-butane, and n-butenes;passing the process stream to a selective hydrogenation unit to generate a selective hydrogenation unit product stream comprising isobutane, isobutene, n-butane, and n-butenes;passing the selective hydrogenation unit product stream to a dehydrogenation fractionation unit to generate a light stream, a heavies stream, and a dehydrogenation fractionation product stream;passing the dehydrogenation fractionation product stream to an alkylation unit to produce an alkylation unit product stream comprising alkylate;passing the alkylation unit product stream to a deisobutanizer to generate a deisobutanizer overhead stream and a deisobutanizer bottoms stream;passing the deisobutanizer bottoms stream to a debutanizer to generate a debutanizer overhead stream and a debutanizer alkylate products stream;passing a portion of the debutanizer overhead stream to an isomerization unit to generate an isomerization unit product stream which is passed to the deisobutanizer; andpassing a portion of the debutanizer overhead stream to the dehydrogenation unit.2. The process of claim 1 , further comprising passing a portion of the debutanizer overhead stream to an isomerization unit to generate an isomerization unit product stream which is passed to the deisobutanizer and passing a portion of the debutanizer overhead stream to the dehydrogenation unit.3. The process of claim 1 , wherein the hydrocarbon stream comprises about 38% ...

ISOPARAFFIN-OLEFIN ALKYLATION

In a process for the catalytic alkylation of an olefin with an isoparaffin, an olefin-containing feed is contacted with an isoparaffin-containing feed under alkylation conditions in the presence of a solid acid catalyst comprising a crystalline microporous material of the MWW framework types, wherein the olefin-containing feed consists essentially of pentenes. 1. A hydrocarbon product produced by isoparaffin-olefin alkylation comprising a Cfraction comprising trimethylpentane isomers and dimethylhexane isomers and a Cfraction comprising trimethylhexane isomers and dimethylheptane isomers , wherein the ratio of trimethylpentane isomers to dimethylhexane isomers is from 3:1 to 22:1 in the Cfraction , wherein the ratio of trimethylhexane isomers to dimethylheptane isomers is from 0.5:1 to 2:1 in the Cfraction.2. The hydrocarbon product of claim 1 , further comprising an isoparaffin Cfraction that makes up between 18-45 wt % of the total C liquids in the hydrocarbon product.3. The hydrocarbon product of claim 1 , further comprising a Cfraction that makes up between 10-50 wt % of the total C liquids in the hydrocarbon product. This application is a divisional application of U.S. patent application Ser. No. 15/610,679, filed on Jun. 1, 2017, which claimed the benefit of U.S. Provisional Application Nos. 62/353,666, 62/353,671, 62/353,675, 62/353,684, and 62/353,687, all filed on Jun. 23, 2016, the entire contents of each are incorporated herein by reference.The present disclosure relates to a process for isoparaffin-olefin alkylation.Alkylation is a reaction in which an alkyl group is added to an organic molecule. Thus an isoparaffin can be reacted with an olefin to provide an isoparaffin of higher molecular weight. Industrially, the concept depends on the reaction of a Cto Colefin with isobutane in the presence of an acidic catalyst producing a so-called alkylate. This alkylate is a valuable blending component in the manufacture of gasoline due not only to its high ...

LIQUID-SOLID AXIAL MOVING BED REACTION AND REGENERATION DEVICE, AND SOLID ACID ALKYLATION METHOD

A liquid-solid axial moving bed reaction and regeneration apparatus and a solid acid alkylation process by using the liquid-solid axial moving bed reaction and regeneration apparatus. the liquid-solid axial moving bed reaction and regeneration apparatus comprise: 1. A liquid-solid axial moving bed reaction and regeneration apparatus , which is characterized in that the apparatus comprises:{'b': 1', '5', '4', '6', '6', '1, 'An axial moving bed reactor (), a spent catalyst receiver (), a catalyst regenerator () and a regenerated catalyst receiver () that are successively connected, wherein, a catalyst outlet of the regenerated catalyst receiver () is communicated with a catalyst inlet of the axial moving bed reactor ();'}{'b': 1', '3', '1', '2', '3, 'Wherein, the axial moving bed reactor () is provided with at least two catalyst beds () arranged up and down, the axial moving bed reactor () is provided with a feed inlet () above each catalyst bed ();'}{'b': 16', '3', '1, 'A catalyst delivery pipe () is arranged between two adjacent catalyst beds () so that the catalyst can move from top to bottom in the axial moving bed reactor ();'}{'b': 10', '3', '10', '16', '10', '10', '16, 'A separation component () is provided between two adjacent catalyst beds (), the separation component () is communicated with a catalyst delivery pipe (), the separation component () is for separating the stream after the reaction in the upstream catalyst bed from the catalyst, the catalyst obtained by the separation with the separation component () moves down through the catalyst delivery pipe ().'}212111. The liquid-solid axial moving bed reaction and regeneration apparatus according to claim 1 , wherein a reaction stream outlet of the last catalyst bed of the axial moving bed reactor () is communicated with the feed inlet () of the first catalyst bed of the axial moving bed reactor () to recycle the reaction stream obtained from the axial moving bed reactor () back to the axial moving bed ...

HYDROCARBON CONVERSION PROCESS INCLUDING CATALYST REGENERATION

A hydrocarbon conversion process is described. The process includes contacting a hydrocarbon feed with an acidic catalyst under hydrocarbon conversion conditions in a hydrocarbon conversion zone. The hydrocarbon feed reacts to form a mixture comprising reaction products, the acidic catalyst, and deactivated acidic catalyst containing conjunct polymer. The mixture is separated into at least two streams, a first stream comprising the reaction products and a second stream comprising the deactivated acidic catalyst. The reaction products are recovered. The deactivated acidic catalyst is contacted with at least one silane or borane compound in a regeneration zone under regeneration conditions, the conjunct polymer reacting with the at least one silane or borane compound resulting in a catalyst phase and an organic phase containing the conjunct polymer and at least one silyl or boryl compound. 1. A hydrocarbon conversion process comprising:contacting a hydrocarbon feed with an acidic catalyst under hydrocarbon conversion conditions in a hydrocarbon conversion zone, the acidic catalyst selected from the group consisting of sulfuric acid, hydrofluoric acid, trifluoromethanesulfonic acid, phosphoric acid, boron trifluoride, and acidic ionic liquids, the hydrocarbon feed reacting to form a mixture comprising reaction products, the acidic catalyst, and deactivated acidic catalyst containing conjunct polymer;separating the mixture into at least two streams, a first stream comprising the reaction products and a second stream comprising the deactivated acidic catalyst containing conjunct polymer;recovering the reaction products;contacting the deactivated acidic catalyst containing the conjunct polymer with at least one silane or borane compound in a regeneration zone under regeneration conditions, the conjunct polymer reacting with the at least one silane or borane compound resulting in a catalyst phase and an organic phase containing the conjunct polymer and at least one silyl ...

HYDROCARBON CONVERSION PROCESSES USING LACTAMIUM-BASED IONIC LIQUIDS

A hydrocarbon conversion process is described. The process involves contacting a hydrocarbon feed with a lactamium based ionic liquid catalyst in a reaction zone under reaction conditions to form a mixture comprising reaction products, and the lactamium based ionic liquid catalyst. Typical hydrocarbon conversion processes include alkylation, oligomerization, isomerization, disproportionation, and reverse disproportionation. 1. A hydrocarbon conversion process comprising:contacting a hydrocarbon feed with a lactamium based ionic liquid catalyst in a hydrocarbon conversion zone under hydrocarbon conversion conditions to form a mixture comprising reaction products, and the lactamium based ionic liquid catalyst.3. The process of wherein an anion of the Brønsted acid HX is at least one of carboxylates claim 2 , nitrates claim 2 , phosphates claim 2 , phosphinates claim 2 , phosphonates claim 2 , imides claim 2 , cyanates claim 2 , borates claim 2 , sulfates claim 2 , sulfonates claim 2 , acetates claim 2 , and halides.4. The process of wherein the ionic liquid has the general formula (III) and wherein at least one ring has at least one C—C double bond.5. The process of wherein the hydrocarbon conversion process comprises at least one of alkylation claim 1 , oligomerization claim 1 , isomerization claim 1 , disproportionation claim 1 , and reverse disproportionation.6. The process of wherein the hydrocarbon conversion conditions include at least one of a temperature in a range of about −20° C. to about 250° C. claim 1 , and a pressure in a range of about 0 MPa (g) to about 7.1 MPa (g).7. The process of further comprising separating the reaction products from the lactamium based ionic liquid catalyst.8. The process of further comprising regenerating the lactamium based ionic liquid catalyst.9. The process of further comprising recycling the regenerated lactamium based ionic liquid to the hydrocarbon conversion zone.10. The process of further comprising adding an acid claim ...

Operation of Modified HF Alkylation Unit

An HF alkylation process for producing gasoline boiling range alkylate product by the alkylation in an HF alkylation unit of a light olefin reactant with an isoparaffin reactant in the presence of a hydrogen fluoride/sulfolane alkylation catalyst mixture in which fresh sulfolane feed having a Total Acid Number (TAN, ASTM D974) not more than 2 mq./L and optimally not more than 1 meq./L. is added to the hydrogen fluoride/sulfolane alkylation catalyst circulating in the unit. Control over the acidic components of the sulfolane feed is appropriately maintained by monitoring and pretreatment with an ion exchange resin to remove acidic components from the feed.

Apparatus for performing a hydrocarbon conversion using an acidic ionic liquid

We provide an apparatus for performing a hydrocarbon conversion or for handling of an output of the hydrocarbon conversion, comprising: a bare metal alloy, wherein the bare metal alloy comprises: from 15.1 to 49 wt % nickel, from 2.3 to 10 wt % molybdenum, from 0.00 to 2.95 wt % copper, from 5 to 25 wt % chromium, and from 20 to 59 wt % iron; wherein the bare metal alloy exhibits a corrosion rate less than 0.07 mm/year when performing the hydrocarbon conversion or handling the output of the hydrocarbon conversion; and wherein the hydrocarbon conversion is performed using an acidic ionic liquid. We also provide a process for using the apparatus.

Optimizing An Alkylation Olefins Source

Alkylate is produced by supplying iso-C hydrocarbon feed to an alkylation reactor, and by further selectively supplying to the alkylation reactor an olefin selected from the group consisting of refinery grade propylene (RGP) and polymer grade propylene (PGP), and combinations thereof. The olefin feed is controlled such that the proportion of PGP supplied through the olefin feed inlet exceeds that of RGP for a predetermined time interval, using a special purpose computer programmed to optimize the allocation of PGP between alkylation production and a commodity market in order to increase total net profit margin. 113-. (canceled)14. A method of optimizing PGP usage , comprising:{'sub': '4+', 'configuring an alkylation unit to produce an effluent comprising alkylate, the alkylate being produced by reacting propylene with a second hydrocarbon, the second hydrocarbon comprising at least one iso-C hydrocarbon;'}configuring one or more propylene sources to supply RGP and/or PGP to the alkylation unit;determining a first value, the first value being generated by producing a preselected alkylate amount from a preselected PGP amount in the alkylation unit;determining a second value, the second value being generated by selling of the preselected PGP amount on a commodity market;comparing the first and second values; andincreasing the PGP supply to the alkylation unit when the first value is greater than the second value.15. The method of claim 14 , wherein (a) the iso-C hydrocarbon comprises isobutane claim 14 , (b) the PGP comprises ≤1.0 wt. % propane claim 14 , and (c) unreacted isobutane is separated from the effluent and recycled to the alkylation unit for additional alkylation without separating additional propane from the unreacted isobutane during the increased PGP supply.16. The method of claim 14 , further comprising (i) decreasing the PGP supply to the alkylation unit when the first value is less than the second value and (ii) maintaining substantially constant the ...

FARNESANE ALKYLATION

An alkylate base oil of biological origin and a process to make an alkylate base oil comprising: a) hydrogenating a farnesene to make a farnesane comprising from zero to less than 5 wt % unsaturated molecules; and b) alkylating the farnesane with one or more C6 to C43 olefins in the presence of an acidic alkylation catalyst to make the alkylate base oil having a kinematic viscosity at 100° C. from 3 mm/s to 20 mm/s. 1. A process to make an alkylate base oil , comprising:a. hydrogenating a farnesene to make a farnesane comprising from zero to less than 5 wt % unsaturated molecules; and{'sup': 2', '2, 'b. alkylating the farnesane with one or more C6 to C43 olefins in the presence of an acidic alkylation catalyst to make the alkylate base oil having a kinematic viscosity at 100° C. from 3 mm/s to 20 mm/s and a viscosity index greater than 80.'}2. The process of claim 1 , wherein the farnesene is of biological origin.3. The process of claim 1 , wherein the farnesene comprises a mixture of isomers.4. The process of claim 1 , wherein the farnesane comprises less than 1 wt % unsaturated molecules.5. The process of claim 1 , wherein the hydrogenating is performed in the presence of a solid supported hydrogenation catalyst with at least one active metal component.6. The process of claim 5 , wherein the at least one active metal component comprises at least one element from the group of Ni claim 5 , Pd claim 5 , Pt claim 5 , Fe claim 5 , Ru claim 5 , Co claim 5 , Rh claim 5 , Cu claim 5 , and Zn.7. The process of claim 1 , wherein the hydrogenating is performed in the presence of a hydrogenation catalyst that contains cobalt or nickel combined with a partially or fully sulfided form of Mo or W.8. The process of claim 1 , wherein the hydrogenating is performed in the presence of an unsupported hydrogenation catalyst.9. The process of claim 1 , wherein the one or more C6 to C43 olefins are linear olefins.10. The process of claim 9 , wherein the one or more C6 to C43 olefins ...

BASE OIL HAVING HIGH VISCOSITY INDEX FROM ALKYLATION OF DIMER KETONE-DERIVED OLEFIN

A process to make an alkylate base oil having a viscosity index greater than or equal to 90, comprising: 1. A process to make an alkylate base oil having a viscosity index greater than or equal to 90 , comprising:a. converting an at least one dimeric ketone to an at least one alcohol;b. dehydrating the at least one alcohol to make one or more corresponding olefins; andc. alkylating at least one isoalkane with the one or more corresponding olefins to form the alkylate base oil.2. The process of wherein the alkylate base oil has the viscosity index greater than or equal to 120.3. The process of claim 1 , wherein the alkylate base oil is an API Group III base oil.4. The process of claim 1 , wherein the alkylate base oil has a kinematic viscosity at 100° C. from 3.0 to 20 mm/s.5. The process of claim 1 , wherein the alkylate base oil has a higher molecular weight claim 1 , a lower pour point claim 1 , and a lower cloud point than the at least one dimeric ketone.6. The process of claim 1 , wherein the alkylate base oil has a bromine index less than 1000 and a kinematic viscosity at 100° C. greater than 3 mm/s.7. The process of claim 1 , wherein the alkylating introduces branching into the alkylate base oil at a central position such that the alkylate base oil has a pour point less than −15° C.8. The process of claim 1 , wherein the at least one dimeric ketone is derived from a biological source.9. Process according to claim 1 , wherein the at least one dimeric ketone is prepared by ketonization of one or more carboxylic acids.10. The process of claim 1 , wherein the converting is done by contacting the at least one dimeric ketone with a hydrogen and a solid hydrogenation catalyst.11. The process of claim 10 , wherein the solid hydrogenation catalyst is a carbon supported metal hydrogenation catalyst.12. The process of claim 11 , wherein the carbon supported metal hydrogenation catalyst comprises from 0.1 to 10 wt % hydrogenation metal claim 11 , and a conversion of the ...

ALKYLATION OF METALLOCENE-OLIGOMER WITH ISOALKANE TO MAKE HEAVY BASE OIL

A process to make an isoalkane alkylate base oil, comprising: 1. A process to make an isoalkane alkylate base oil , comprising:a. oligomerizing an olefin feed having a carbon number from 3 to 6 using a metallocene catalyst to make an unsaturated olefin oligomer; and{'sup': '2', 'b. alkylating an isoalkane feed with the unsaturated olefin oligomer in the presence of an acidic alkylation catalyst, and without any addition of hydrogen, to make an alkylate product comprising the isoalkane alkylate base oil having a kinematic viscosity at 100° C. greater than 10 mm/s, a VI higher than 80, and a bromine index less than 1000 mg Br/100 g.'}2. The process of claim 1 , additionally comprising distilling the alkylate product and collecting the isoalkane alkylate base oil and a middle distillate.3. The process of claim 1 , wherein the isoalkane feed comprises isobutane claim 1 , isopentane claim 1 , hydrocracker naphtha claim 1 , or mixtures thereof.4. The process of claim 1 , wherein the olefin feed comprises a propylene claim 1 , a butene claim 1 , or a mixture thereof.5. The process of claim 1 , wherein the metallocene catalyst comprises a metallocene complex containing a transition metal selected from the group consisting of titanium (Ti) claim 1 , zirconium (Zr) claim 1 , hafnium claim 1 , (Hf) claim 1 , and combinations thereof.6. The process of claim 1 , wherein the metallocene catalyst comprises a substituted cyclopentadienyl ligand.7. The process of claim 1 , wherein the metallocene catalyst comprises an aluminoxane activator.8. The process of claim 1 , wherein the metallocene catalyst comprises bis(t-butylcyclopentadienyl)zirconium dichloride and MAO.9. The process of claim 1 , wherein the oligomerizing is performed under a hydrogen pressure from 200 to 5000 kPa.10. The process of claim 1 , wherein the olefin feed comprises an inert hydrocarbon solvent.11. The process of claim 1 , wherein the acidic alkylation catalyst is selected from the group consisting of an ...

HIGH VISCOSITY INDEX LUBRICANTS BY ISOALKANE ALKYLATION

An isoalkane alkylate base oil and a process to make an isoalkane alkylate base oil having a VI higher than 90, comprising: 1. A process to make an isoalkane alkylate base oil having a VI higher than 90 , comprising:{'sub': 'alkane+olefin', 'a. selecting an isoalkane feed containing at least one isoalkane and an olefin feed containing at least one linear olefin such that a combined carbon number of the isoalkane feed and the olefin feed (N) is from 20 to 60; and'}b. alkylating the isoalkane feed with the olefin feed in the presence of an acidic alkylation catalyst under alkylation conditions to make the isoalkane alkylate base oil having the VI higher than 90;{'sup': '2', 'wherein the isoalkane alkylate base oil has a kinematic viscosity at 100° C. from 2 to 30 mm/s, a pour point less than 0° C., and a bromine index less than 2000 mg Br/100 g.'}2. The process of claim 1 , wherein the isoalkane feed has a feed isoalkane carbon number (N) of 6 to 50 and the olefin feed has a linear olefin carbon number (N) of 10 to 43.3. The process of claim 1 , wherein the at least one linear olefin comprises an internal olefin.4. The process of claim 3 , additionally comprising isomerizing an alpha olefin to make the internal olefin.5. The process of claim 1 , wherein the at least one linear olefin is an alpha olefin.6. The process of claim 1 , wherein the olefin feed is of biological origin.7. The process of claim 1 , wherein the acidic alkylation catalyst is selected from the group consisting of an acidic ionic liquid claim 1 , a sulfuric acid claim 1 , a hydrofluoric acid claim 1 , a triflic acid claim 1 , another Brønsted acid with a Hammet acidity function less than −10 (H<−10) claim 1 , an acidic zeolite claim 1 , a sulfated zirconia claim 1 , and a tungstated zirconia.8. The process of claim 1 , wherein the acidic alkylation catalyst comprises an ionic liquid and a Brønsted acid.9. The process of claim 8 , wherein the ionic liquid is a chloroaluminate and the Brønsted acid is ...

System And Producing Method for Preparing Oil By Using Sulfuric Acid As Catalyst

Disclosed are a system device for preparing an alkylate oil using a sulfuric acid catalyst and a manufacturing method thereof. The system device comprises a reactor unit (), a catalyst and hydrocarbon circulation unit (), a separator unit (), an isobutane circulation unit () and a fractionator unit (). The reactor unit () is connected and in communication with the catalyst and hydrocarbon circulation unit () and the separator unit () via channels respectively. The catalyst and hydrocarbon circulation unit () is connected and in communication with the separator unit () via channels. The separator unit () is connected and in communication with the isobutane circulation unit () and the fractionator unit () via channels respectively. The catalyst and hydrocarbon circulation unit (), the separator unit (), the isobutane circulation unit () and the fractionator unit () are connected and in communication with the reactor unit () via channels respectively. The reactor unit () comprises at least a high gravity reactor. Due to the adopted high gravity reactor capable of highly reinforcing the mixing of materials under high viscosity, the system device can operate at a low temperature of −5° C. and prepare the alkylate oil having an octane number of 97-100 at an alkane/alkene ratio of 2-100. 1. A system for preparing alkylated oil by using sulfuric acid as a catalyst , comprising a reactor unit , a catalyst and hydrocarbon circulating unit , a separator unit , an isobutene circulating unit and a fractionator unit;wherein the reactor unit is respectively communicated with the catalyst and hydrocarbon circulating unit and the separator unit through pipes; the catalyst and hydrocarbon circulating unit is communicated with the separator unit through a pipe; the separator unit is respectively communicated with the isobutene circulating unit and the fractionator unit through pipes; the catalyst and hydrocarbon circulating unit, the separator unit, the isobutene circulating unit and ...

ISOPARAFFIN-OLEFIN ALKYLATION

In a process for the catalytic alkylation of an olefin with an isoparaffi, an olefin-containing feed is contacted with an isoparaffin-containing feed under alkylation conditions in the presence of a solid acid catalyst comprising a crystalline microporous material of at least one of the MWW and MOR framework types, wherein the solid acid catalyst is substantially free of amorphous alumina. 1. A process for the catalytic alkylation of an olefin with an isoparaffin comprising , the process comprising: contacting an olefin-containing feed with an isoparaffin-containing feed under alkylation conditions in the presence of a solid acid catalyst comprising a crystalline microporous material of at least one of the MWW and MOR framework types , wherein the solid acid catalyst is substantially free of a binder containing amorphous alumina.2. The process of claim 1 , wherein the solid acid catalyst is substantially binder-free.3. The process of claim 1 , wherein the solid acid catalyst comprises a binder comprising a crystalline molecular sieve.4. The process of claim 1 , wherein the solid acid catalyst comprises at least one of a silica claim 1 , titania claim 1 , and zirconia binder.5. The process of claim 1 , wherein the solid acid catalyst comprises a crystalline microporous material of the MWW framework type.6. The process of claim 5 , wherein the crystalline microporous material of the MWW framework type is selected from the group consisting of MCM-22 claim 5 , PSH-3 claim 5 , SSZ-25 claim 5 , ERB-1 claim 5 , ITQ-1 claim 5 , ITQ-2 claim 5 , MCM-36 claim 5 , MCM-49 claim 5 , MCM-56 claim 5 , EMM-10 claim 5 , EMM-12 claim 5 , EMM-13 claim 5 , UZM-8 claim 5 , UZM-8HS claim 5 , UZM-37 claim 5 , MIT-1 claim 5 , and mixtures thereof.7. The process of claim 5 , wherein the crystalline microporous material of the MWW framework type comprises MCM-49.8. The process of claim 5 , wherein the MWW framework type material contains up to 10% by weight of impurities of other framework ...

Method of regeneration of a spent sulfuric acid catalyst from alkylation of olefins and alkanes via paired oxidation

A spent sulfuric acid catalyst from an alkylation unit is regenerated via a paired oxidation electrolysis, wherein active intermediates are generated via both anodic oxidation and cathodic reduction without adding an additional organic peroxide during the electrolysis. The organic impurities in the spent sulfuric acid catalyst are decomposed by the active intermediates, and removed therefrom via evaporation. 1. A method of regeneration of a spent sulfuric acid catalyst from alkylation of olefins and alkanes , said spent sulfuric acid catalyst containing organic impurities and water , said method comprising introducing said spent sulfuric acid catalyst into an electrolysis reactor containing an anode and a cathode , introducing air or O-containing gas into said spent sulfuric acid catalyst , and supplying electricity to said anode and said cathode , wherein the improvement comprises said cathode being O-diffusion cathode , and said air or O-containing gas being introduced into said spent sulfuric acid catalyst through the O-diffusion cathode , so that oxygen , and water and protons in the spent sulfuric acid catalyst undergo reduction reactions at the O-diffusion cathode , forming oxidants of hydrogen peroxide and hydroxyl free radicals , and thus at least a portion of the organic impurities are decomposed via reactions with oxygen and the so-formed oxidants.2. The method of wherein no organic peroxide is added to said spent sulfuric acid catalyst before or during said supply of electricity.3. The method of claim 1 , wherein said anode comprises a semiconductor photocatalyst claim 1 , and a photo energy or light radiation having a wavelength of 10 to 2000 nm is applied to said anode.4. The method of claim 3 , wherein said semiconductor photocatalyst comprises a metal oxide semiconductor.5. The method of claim 3 , wherein said semiconductor photocatalyst comprises Ti—TiO claim 3 , or TiO.6. The method of claim 1 , wherein said anode comprises platinum claim 1 , ...

FLEXIBLE PRODUCTION OF GASOLINE AND JET FUEL IN ALKYLATION REACTOR

Systems and processes for the flexible production of gasoline and jet fuel via alkylation of C4 and C5 olefins. 1. A system for flexible production of gasoline and jet fuel , the system comprising:an alkylation reaction zone comprising one or more reactors for reacting C4 olefins, C5 olefins, C6 olefins, C4-C5 olefins, or C4-C6 olefins with C4-C6 isoparaffins in the presence of sulfuric acid alkylation catalyst to produce a hydrocarbon effluent and a spent acid stream;a flow line for providing C4 olefins to the alkylation reaction zone;a flow line for providing C5 olefins to the alkylation reaction zone;a flow line for providing fresh acid alkylation catalyst to the alkylation reaction zone;a deisobutanizer for separating the hydrocarbon effluent into an isobutane fraction, a n-butane fraction, and a C5+ fraction;a deisopentanizer for separating the C5+ fraction into an isopentane fraction and a C6+ fraction;a splitter for separating the C6+ fraction into a light alkylate overhead fraction and a heavy alkylate bottoms fraction;a flow system for recycling the isobutane fraction to the alkylation reaction zone, recovering the isobutane fraction as an isobutane product, and both recycling a portion of the isobutane fraction to the alkylation reaction zone and recovering a portion of the isobutane fraction as an isobutane product;a flow system for recycling the isopentane fraction to the alkylation reaction zone, recovering the isopentane fraction as an isopentane product, and both recycling a portion of the isopentane fraction to the alkylation reaction zone and recovering a portion of the isopentane fraction as an isopentane product;a flow system for recycling the light alkylate fraction to the alkylation reaction zone, recovering the light alkylate as a light alkylate product, and both recycling a portion of the light alkylate fraction to the alkylation reaction zone and recovering a portion of the light alkylate fraction as a light alkylate product.2. The system of ...

Ionic liquid catalyst having enhanced activity

A process for producing acidic ionic liquid catalyst having enhanced activity comprising combining fresh acidic ionic liquid catalyst, a metal and a Broensted acid in a reaction zone for a time sufficient to increase the activity of the ionic liquid catalyst is disclosed. A process for producing acidic ionic liquid catalyst having enhanced activity comprising the steps of combining fresh ionic liquid catalyst, a metal and HCl in a reaction zone for a time sufficient to increase the activity of the fresh ionic liquid catalyst; removing reaction product from the reaction zone and recovering at least a portion of the treated ionic liquid catalyst is also disclosed.

Catalyst, process for making thereof as well as process for the alkylation of aliphatic hydrocarbons with olefins

Material à base de sílica e processo para sua preparação, processo para a alquilação de um hidrocarboneto alifático e processo para regenerar um catalisador

Process for the regeneration of an alkylation catalyst

PROCEDURE FOR THE RENTAL OF PARAFFINS.

LA INVENCION CONCIERNE A UN PROCESO DE ALQUILACION EN EL CUAL SE TRATA UNA CARGA QUE COMPRENDE AL MENOS UNA ISOPARAFINA Y AL MENOS UNA OLEFINA QUE CONTIENE DE 2 A 6 ATOMOS DE CARBONO POR MOLECULA, EN PRESENCIA DE UN CATALIZADOR SOLIDO DE ALQUILACION; DICHO PROCESO COMPRENDE: A) LA INTRODUCCION Y LA PUESTA EN CONTACTO CON EL CATALIZADOR PRESENTE EN UNA ZONA REACCIONAL R DE LOS COMPUESTOS SIGUIENTES: (I) DICHA CARGA, PREFERENTEMENTE INTRODUCIDA AL MENOS EN LA ENTRADA DE LA ZONA R; (II) EL EFLUENTE LIQUIDO DESCRITO EN B), INTRODUCIDO AL MENOS EN LA ENTRADA DE LA ZONA R, PREFERENTEMENTE EN SU TOTALIDAD INTRODUCIDOS EN LA ENTRADA DE LA ZONA R Y, (III) EL EFLUENTE LIQUIDO DESCRITO EN D), PREFERENTEMENTE INTRODUCIDO AL MENOS EN LA ENTRADA DE LA ZONA R; B) EL RECICLAJE DE UNA PARTE DEL EFLUENTE LIQUIDO QUE SALE DE LA ZONA REACCIONAL R HACIA LA ENTRADA DE DICHA ZONA R; C) LA INTRODUCCION DE OTRA PARTE DEL EFLUENTE LIQUIDO QUE SALE DE LA ZONA REACCIONAL R EN UNA ZONA DE SEPARACION ISOBUTANO/NORMAL-BUTANO/ALQUILATO S; D) EL RECICLAJE DE LA MAYOR PARTE DEL EFLUENTE LIQUIDO RICO EN ISOBUTANO DE LA ZONA S EN ZONA REACCIONAL R; E) LA OBTENCION DE UN ALQUILATO COMO PRODUCTO, EXTRAIDO DE LA PARTE INFERIOR EN LA ZONA S, Y F) LA OBTENCION DE NORMAL-BUTANO COMO PURGA DE LA ZONA S, EL PROCESO ESTA CARACTERIZADO POR EL EMPLEO DE UN CATALIZADOR ESPECIFICO EN PARTICULAR COMPRENDIENDO ACIDO SULFURICO IMPREGNADO SOBRE UN SOPORTE POROSO. THE INVENTION CONCERNS A RENTING PROCESS IN WHICH A LOAD IS TREATED, INCLUDING AT LEAST ONE ISOPARAPHINE AND AT LEAST ONE OLEPHINE CONTAINING 2 TO 6 CARBON ATOMS PER MOLECULA, IN THE PRESENCE OF A SOLID RENTAL CATALYST; SUCH PROCESS INCLUDES: A) THE INTRODUCTION AND CONTACT WITH THE CATALYST PRESENT IN A REACTIONAL ZONE R OF THE FOLLOWING COMPOUNDS: (I) SUCH LOAD, PREFERABLY INTRODUCED AT LEAST AT THE ENTRANCE OF ZONE R; (II) THE EFFLUENT LIQUID DESCRIBED IN B), INTRODUCED AT LEAST IN THE ENTRANCE OF ZONE R, PREFERABLY IN ITS ENTIRETY INTRODUCED IN THE ...

HF alkylation process with internal acid regeneration

An improved process for removing polymeric by-product (ASO) from the HF alkylation acid in an HF alkylation unit used for the production of gasoline boiling range alkylate product by olefin/iso-paraffin alkylation, comprises fractionating a portion of the circulating HF alkylation acid inventory of the unit with a portion of hot alkylate product in a fractionation zone to from an overhead product comprising HF alkylation acid and water and a bottoms fraction comprising the polymeric by-product and alkylate. The bottoms fraction is sent to the isoparaffin stripper of the unit to remove trace HF alkylation acid as overhead and form a product stream of hot alkylate as a bottoms fraction.

Isoparaffin-olefin alkylation utilizing a membrane to separate olefins from a feed stream

This invention relates to an improved process for the alkylation of olefins in an alkylation unit feed stream in order to produce a higher yield of alkylate having a higher octane number, a lower acid consumption rate, and a lower energy consumption. Such a process involves passing a feed stream comprised of olefins and paraffins through a membrane so that the olefins are separated from the paraffins. In passing through the membrane, the olefins are facilitated in their transport by an isoparaffin sweep stream and together, the olefin/isoparaffin stream is passed into an alkylation reactor. Within the reactor, the olefins react with the isoparaffins to form alkylate.

Paraffin alkylation

A process for paraffin alkylation of isoalkane with isoolefins in which an olefin component comprising oligomerized propylene, oligomerized isoolefin or mixtures thereof is fed to a paraffin alkylation unit wherein the dissociated olefin components forming the oligomers react with isoalkane to produce a reaction mixture containing an alkylate and unreacted isoalkane The reaction mixture is fractionally distilled to recover unreacted isoalkane as overheads and alkylate as bottoms. The stoichiometry of isoolefins to isoalkane in the alkylation unit is maintained by adjustment of the feed to the oligomerization, for example, by adding fresh isoalkane to the recovered, unreacted isoalkane from the alkylation unit being recycled to the oligomerization. Alternatively, a portion of the recovered unreacted isoalkane is dehydrogenation to an isoolefin which is added to the oligomerization.

Paraffin alkylation

A process for paraffin alkylation of isoalkane with isoolefins in which an olefin component comprising oligomerized propylene, oligomerized isoolefin or mixtures thereof is fed to a paraffin alkylation unit wherein the dissociated olefin components forming the oligomers react with isoalkane to produce a reaction mixture containing an alkylate and unreacted isoalkane The reaction mixture is fractionally distilled to recover unreacted isoalkane as overheads and alkylate as bottoms. The stoichiometry of isoolefins to isoalkane in the alkylation unit is maintained by adjustment of the feed to the oligomerization, for example, by adding fresh isoalkane to the recovered, unreacted isoalkane from the alkylation unit being recycled to the oligomerization. Alternatively, a portion of the recovered unreacted isoalkane is dehydrogenation to an isoolefin which is added to the oligomerization.

Ionic liquid reactor with heat exchanger

An ionic liquid reactor unit and a process for controlling heat generation from an ionic liquid reactor unit. The ionic liquid reactor unit may include an external heat exchanger. The effluent from the reactor is separated in a separation zone allowing the hydrocarbon phase to transfer heat to a cooling fluid. The heat exchanger may be a tube-in-shell, a spiral plate heat exchanger, a hair pin heat exchanger. The heat exchanger accommodates the separation of the ionic liquid from the hydrocarbon phase, and may allow for the ion liquid to be drained.

Alkylation aid

Alkylation catalyst of the type used in the refining of petroleum can be improved by using a promoter composition which contains an alkyl phosphate ester amine salt and pinene.

System and process for alkylation

A method for alkylating a hydrocarbon comprising at least one isoparaffin and at least one olefin by introducing liquid acid catalyst and the hydrocarbon into a high shear reactor, forming an emulsion comprising droplets comprising hydrocarbon in a continuous acid phase, wherein the droplets have a mean diameter of less than about 5 microns, introducing the emulsion into a vessel operating under suitable alkylation conditions whereby at least a portion of the isoparaffin is alkylated with the olefin to form alkylate, and removing a product stream comprising alkylate from the vessel. A system for carrying out the method is also disclosed.

Ionic liquid reactor with heat exchanger

An ionic liquid reactor unit and a process for controlling heat generation from an ionic liquid reactor unit. The ionic liquid reactor unit may include an external heat exchanger. The effluent from the reactor is separated in a separation zone allowing the hydrocarbon phase to transfer heat to a cooling fluid. The heat exchanger may be a tube-in- shell, a spiral plate heat exchanger, a hair pin heat exchanger. The heat exchanger accommodates the separation of the ionic liquid from the hydrocarbon phase, and may allow for the ion liquid to be drained.

Alkylation aid

Alkylation processes of the type used in the refining of petroleum can be improved by using a promoter composition which contains an alkyl phosphate ester amine salt and pinene.

Method for regeneration of acid catalyst

FIELD: alkylation catalysts. SUBSTANCE: regeneration of catalyst used in the process of alkylation of alifatic hydrocarbons includes reagent treatment of liquid phase of catalyst oil formed as by-product during the alkylation process. Hydrogen is used as reagent. Treatment is carried out in presence of catalyst containing at least one VIII group metal (platinum, palladium, or their mixtures) deposited on acid-resistant carrier. The latter may be silicon dioxide, zeolite, or activated carbon. Temperature of treatment ranges from 20 to 200 C, and partial pressure of hydrogen from 1 to 150 bar. EFFECT: increased economical efficiency of process due to regeneration of exhausted part of catalyst. 3 cl, 4 tbl, 2 ex (19) 13) ВИ” 2 122 991 ‹' (51) МПК СЛ С 07С 2/62, В 01 4 27/32, 38/10//(В 01 4 27/32, 103:66, 103:68, 101:42, 101:90, 105:12) Гебсс тс ПЧ Го РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 94023252/04, 06.07.1994 (30) Приоритет: 06.07.1993 ОК 0813/93 (46) Дата публикации: 10.12.1998 (56) Ссылки: ЕР 0433954 АЛ, 26.06.91. ЗЦ 587855 (71) Заявитель: Хальдор Топсеэ А/С (ОК) (72) Изобретатель: Свен Ивар Хоммельтофт (ОК), Клаус Якобсен (ОК) (73) Патентообладатель: 1567835 А, 21.05.80. ОЕ 2547838 АЛ, С) 08.07.76. ЕР 0384457 АЛ, 29.08.90. (54) СПОСОБ РЕГЕНЕРАЦИИ ОТРАБОТАННОГО КИСЛОТНОГО КАТАЛИЗАТОРА = (57) Реферат: нанесенный на устойчивый к воздействию с Изобретение относится к каталитическим кислоты носитель. Катализатор содержит по процессам алкилирования алифатических меньшей мере один металл из группы, © углеводородов, в частности к способу включающей платину, палладий и их смеси. © регенерации отработанного КИСЛОТНОГО Носитель выбран из группы, включающей катализатора, применяемого для двуокись кремния, цеолиты и активированный с алкилирования углеводородов. Способ уголь. Обработку водородом осуществляют регенерации включает обработку реагентом при 20-200°С и парциальном давлении = ...

Isoparaffin-olefin alkylation

A composition comprising a base component and a polymer, and a method of making said composition, are disclosed. The composition thereby obtained is then used as a catalyst for isoparaffin-olefin alkylation.

Isoparaffin-olefin alkylation

A composition comprising a base component and a polymer, and a method of making said composition, are disclosed. The composition thereby obtained is then used as a catalyst for isoparaffin-olefin alkylation.

Isoparaffin-Olefin Alkylation

A composition comprising a base component and a polymer, and a method of making said composition, are disclosed. The composition thereby obtained is then used as a catalyst for isoparaffin-olefin alkylation.

Isoparaffin-Olefin alkylation

A composition comprising a base component and a polymer, and a method of making said composition, are disclosed. The composition thereby obtained is then used as a catalyst for isoparaffin-olefin alkylation.

Paraffin alkylation

A liquid acid process is disclosed in which a hydrocarbon component containing an olefin, an olefin precursor or mixture and an isoalkane and a liquid acid catalyst is fed to a downflow reaction zone containing a disperser, under conditions to induce pulse flow at or near the outlet to react the isoalkane and olefin to produce a reaction product and feeding the reaction product to a vaporization zone containing a disperser under conditions to induce pulse flow at or near the outlet of the vaporization zone. A pressure drop across the disperser in the vaporization zone causes partial vaporization of the hydrocarbon which quench es the heat reaction and cooling the unvaporized portion of said reaction product, which is recovered and allowed to separate into an acid phase and hydrocarbon phase containing the alkylate. The acid catalyst and hydrocarbons may be fractally fed to the reaction zone.

Alkylation process unit with recyle of hydrogen and recovery of hydrogen chloride

We provide alkylation process units, one comprising: a) a hydrogenation reactor that produces a regenerated catalyst effluent; b) a fractionation unit that separates the effluent into gas and light hydrocarbon; c) a connection between the fractionation unit for transmitting the gas to the hydrogenation reactor; and d) a connection between the fractionation unit and an alkylation reactor to transmit the light hydrocarbon to the alkylation reactor. The other comprising: a) a separator, connected between the hydrogenation reactor and a fractionation unit; that separates the effluent into gas and liquid; and wherein the fractionation unit separates a hydrocarbon stream from the liquid into a light hydrocarbon comprising a hydrogen chloride and an extracted conjunct polymer naphtha; b) a connection between the separator and the hydrogenation reactor for transmitting the gas to the hydrogenation reactor; and c) a connection between the fractionation unit and an alkylation reactor to transmit the light hydrocarbon.

Alkylation process with recycle of hydrogen and recovery of hydrogen chloride

We provide processes, and process units for practicing the processes, comprising a. regenerating a used catalyst comprising an ionic liquid catalyst and a chloride, from an alkylation reactor, in a hydrogenation reactor to produce a regenerated catalyst effluent; b. separating at least a portion of the regenerated catalyst effluent into a gas fraction comprising a hydrogen gas and into a light hydrocarbon fraction comprising a hydrogen chloride; c. recycling at least a part of the gas fraction comprising the hydrogen gas to the hydrogenation reactor; and d. recovering at least an amount of the light hydrocarbon fraction comprising the hydrogen chloride and recycling the at least the amount of the light hydrocarbon fraction to the alkylation reactor. The alkylation process units comprise a hydrogenation reactor, a fractionation unit, and connections for transmitting the gas fraction to the hydrogenation reactor and for transmitting the light hydrocarbon fraction to the alkylation reactor.

supported liquid phase ionic liquid catalyst process

processo de catalisador líquido iônico de fase líquida suportada. um processo, compreendendo: a) introduzir um líquido iônico acídico em um reator compreendendo um suporte sólido; b) alimentar ao reator um fluxo de alimentação compreendendo um ácido de bronsted e uma mistura de hidrocarbonetos compreendendo: i. pelo menos um hidrocarboneto alquilável e ii.pelo menos um agente alquilante; e c) coletar um ou mais produtos de hidrocarbonetos líquidos em um efluente do reator, em que o um ou mais produtos de hidrocarbonetos líquidos são produtos de oligômero, produtos alquilados, ou misturas dos mesmos, feitos a partir do hidrocarboneto alquilável. também um processo, compreendendo: a) introduzir um líquido iônico acídico em um reator compreendendo um suporte sólido; b) alimentar ao reator um fluxo de alimentação compreendendo um ácido de bronsted e uma mistura de hidrocarbonetos; c) resfriar o reator porevaporação de um hidrocarboneto volátil de uma zona de reação no reator; e d) coletar um ou mais produtos de hidrocarbonetos líquidos feitos a partir da mistura de hidrocarbonetos. supported liquid phase ionic liquid catalyst process. a process comprising: a) introducing an acidic ionic liquid into a reactor comprising a solid support; b) feeding the reactor a feed stream comprising a bronsted acid and a hydrocarbon mixture comprising: i. at least one alkylatable hydrocarbon and at least one alkylating agent; and c) collecting one or more liquid hydrocarbon products in a reactor effluent, wherein the one or more liquid hydrocarbon products are oligomer products, alkylated products, or mixtures thereof, made from the alkylable hydrocarbon. also a process comprising: a) introducing an acidic ionic liquid into a reactor comprising a solid support; b) feeding to the reactor a feed stream comprising a bronsted acid and a hydrocarbon mixture; c) cooling the reactor by evaporating a volatile hydrocarbon from a reaction zone in the reactor; and d) collecting one or more liquid ...

A process for isomerisation or alkylation a hydrocarbon

How to alkylate aliphatic hydrocarbons with olefins

실리카-기초물질 촉매반응된 올레핀 이용 지방족 탄화수소의 알킬화 방법은 실리카의 표면 Si-OH기를 플루오르알킬술폰산 CF 3 (CF 2 ) n SO 3 H으로 에스테르화하고 여기서 n이 0 내지 11의 정수이며 해밋(Hammett) 산도가 Ho≤-11.4인 것을 특징으로 한다. The process for alkylating aliphatic hydrocarbons using silica-based catalyzed olefins esterifies the surface Si-OH groups of silica with fluoroalkylsulfonic acid CF 3 (CF 2 ) n SO 3 H, where n is an integer from 0 to 11 Hammett) acidity is characterized by Ho≤-11.4.

올레핀 함유 지방족 탄화수소의 알킬화 방법

실리카-기초물질 촉매반응된 올레핀 이용 지방족 탄화수소의 알킬화 방법은 실리카의 표면 Si-OH기를 플루오르알킬술폰산 CF 3 (CH 2 ) n SO 3 H으로 에스테르화하고 여기서 n이 1내지 11의 정수이며 해밋(Hammett) 산도가 Ho≤-11.4인 것을 특징으로 한다.

Материал на основе двуокиси кремния, способ получения материала, способ получения катализатора, способ алкилирования алифатического углеводорода, способ регенерации катализатора

Способ алкилирования алифатических углеводородов олефинами, катализируемый материалом на основе двуокиси кремния, при этом поверхностные группы Si-ОН двуокиси кремния этерифицируют фторалкилсульфокислотой формулы CF 3 (CF 2 ) n SO 3 H, где n - целое число от 0 до 11, при этом упомянутый материал имеет кислотность по Хаммету H o ≤ -11,4. Указанный катализатор проявляет не только превосходные каталитические свойства, превосходящие таковые при использовании трифторметансульфокислоты, адсорбируемой на двуокиси кремния, но обладает также значительной устойчивостью во времени и при этом его легко можно регенерировать. 6 c. и 25 з.п.ф-лы, 6 табл. с6сэ9сЬс ПЧ Го (19) РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ ВИ "” 2126 295' (51) МПК 13) С1 В 01 . 21/08, 31/02, 37/04, С 07 С 2/62, В 01 4 38/02, 38/48 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 94028658/04, 05.08.1994 (30) Приоритет: 06.08.1993 ПТ М 193АО01796 (46) Дата публикации: 20.02.1999 (56) Ссылки: ЕР 0433954 АЛ, 26.06.91. ЗЦ 1598855 АЗ, 07.10.90. 4$ 3970721 А, 20.07.16. $ 4118433 А, 03.10.18. (98) Адрес для переписки: 103735 Москва, ул.Ильинка 5/2, Союзпатент (71) Заявитель: Эниричерке С.п.А. (1Т), Аджип Петроли С.п.А. (1Т) (72) Изобретатель: Марио Габриэле Клеричи (1Т), Карло Перего (1Т), Альберто Де Ангелис (ГГ), Лучано Монтанари (1Т) (73) Патентообладатель: Эниричерке С.п.А. (1Т), Аджип Петроли С.п.А. (1Т) (54) МАТЕРИАЛ НА ОСНОВЕ ДВУОКИСИ КРЕМНИЯ, СПОСОБ ПОЛУЧЕНИЯ МАТЕРИАЛА, СПОСОБ ПОЛУЧЕНИЯ КАТАЛИЗАТОРА, СПОСОБ АЛКИЛИРОВАНИЯ АЛИФАТИЧЕСКОГО УГЛЕВОДОРОДА, СПОСОБ РЕГЕНЕРАЦИИ КАТАЛИЗАТОРА (57) Реферат: Способ алкилирования алифатических углеводородов олефинами, катализируемый материалом на основе двуокиси кремния, при этом поверхностные группы $-ОН двуокиси кремния этерифицируют фторалкилсульфокислотой формулы СЕ з(СЕ2)-ОЗН, где п - целое число от 0 до 11, при этом упомянутый материал имеет кислотность по Хаммету Но < -114. Указанный катализатор проявляет не только превосходные ...

하나이상의 c_3-c_6 올레핀에 의해 c_4-c_5 이소파라핀을 알킬화시키기 위한 촉매

본 발명은 황산 및 화합물 HB(HSO 4 ) 4 로 구성된 산 상 및 상기 산 상으로 함침시킨 실리카를 함유하며, 상기 산 상으로 함침시키기 전의 실리카의 총공극 부피는1g당 0.1내지 0.6㎤이며, 상기 산 상은 0.4중량%내지 68.8중량%의 화합물 HB(HSO 4 ) 4 및 31.2중량% 내지 99.6중량의 화합물 H 2 SO 4 를 포함하며, 상기 산 상이 황산 무수물 또는 붕산을 함유하지 않는 것을 특징으로 하는 평균 직경이 0.1내지 30㎛인 입자로 거의 구성된 촉매에 관한 것이다. 또한, 본 발명은 분자당 하나이상의 C 3 -C 6 올레핀의 존재하에 이소부탄 및/또는 이소펜탄을 촉매 알킬화시키는데 있어서의 촉매의 제조 방법 및 촉매의 사용 방법에 관한 것이다.

Method of and apparatus for controlling an alkylation process

Disclosed is a method of alkylating in which a hydrocarbon and acid emulsion is circulated in a reaction loop between a reactor and a cooler. A small sidestream of the reaction emulsion is constantly removed to a liquid-liquid separator where the hydrocarbon and acid phases are separated. The recovered acid is then recycled back to the reaction loop. The amount of recovered acid recycled is controlled by monitoring the density of the reaction emulsion.

一种异构烷烃与烯烃的烷基化方法

本发明涉及一种异构烷烃与烯烃的烷基化方法，其特征在于使用至少二个并联的反应器，当其中一个或多个反应器中的催化剂需要再生时，在反应器原位通过溶剂与固体酸催化剂接触，冲洗清除覆盖在固体酸催化剂表面上的大分子烃类，恢复催化剂的高选择性。

一种固体酸催化异构烷烃与烯烃的烷基化反应方法

本发明公开了一种固体酸催化异构烷烃与烯烃的烷基化反应方法，是将包括C 4 -C 6 异构烷烃、C 3 -C 6 单键烯烃和作为反应助剂的强电负性元素化合物在内的反应物料与固体酸催化剂接触进行烷基化反应，其特征在于所说的固体酸催化剂在与反应物料接触前，先与含强电负性元素化合物的异构烷烃接触。该方法使烷基化反应目的产物的选择性大大提高，同时也可以提高固体酸催化剂的稳定性。

수소의 재순환 및 염화수소의 회수를 수반하는 알킬화 공정

본 발명자들은 하기 단계를 포함하는 공정, 및 상기 공정을 실행하기 위한 공정 장치를 제공한다: a. 알킬화 반응기로부터의, 이온성 액체 촉매 및 염화물을 포함하는 사용된 촉매를, 수소화 반응기에서 재생시켜, 재생된 촉매 유출물(regenerated catalyst effluent)을 생성하는 단계; b. 상기 재생된 촉매 유출물의 적어도 일부를, 수소 기체를 포함하는 기체 분획물(gas fraction comprising a hydrogen gas)과 염화수소를 포함하는 경질 탄화수소 분획물(light hydrocarbon fraction comprising a hydrogen chloride)로 분리하는 단계; c. 상기 수소 기체를 포함하는 기체 분획물의 적어도 일부를 상기 수소화 반응기로 재순환시키는 단계; 및 d. 상기 염화수소를 포함하는 경질 탄화수소 분획물의 적어도 일부 양을 회수하고, 상기 경질 탄화수소 분획물의 적어도 일부 양을 상기 알킬화 반응기로 재순환시키는 단계. 본 알킬화 공정 장치(alkylation process units)는 수소화 반응기, 분류 장치, 및 기체 분획물을 수소화 반응기로 전송하고 경질 탄화수소 분획물을 알킬화 반응기로 전송하기 위한 연결부들을 포함한다.

回收废酸催化剂的方法

一种从烷基化流出物流的含水萃取物中回收磺酸催化剂的方法，包括如下步骤： 蒸发萃取物，得到磺酸催化剂的水合物； 水合物与含烯烃的烃物流反应，产生其相应的磺酸酯；和 在烷基化条件下，将酸酯引入到烃原料与烯属烷基化剂的烷基化过程中，在烷基化过程中，磺酸酯分解成具有催化活性的酸形式。

RECOVERY OF EXHAUSTED ACID CATALYST FROM THE RENTAL OF HYDROCARBONS.

SE PRESENTA UN METODO PARA LA RECUPERACION DE UN CATALIZADOR ACIDO A PARTIR DE ACEITE SOLUBLE EN ACIDO QUE SE FORMA EN UN PROCESO PARA LA ALQUILACION DE HIDROCARBONOS Y QUE CONTIENE CANTIDADES VALIOSAS DE CATALIZADOR ACIDO AGOTADO, DICHO METODO COMPRENDE: EL TRATAMIENTO DEL ACEITE SOLUBLE EN ACIDO CON HIDROGENO EN LA PRESENCIA DE UN CATALIZADOR QUE COMPRENDA UNO O MAS METALES ESCOGIDOS ENTRE EL GRUPO VIII DE LA TABLA PERIODICA SOPORTADOS EN UN PORTADOR RESISTENTE AL ACIDO; Y EL TRATAMIENTO DEL ACEITE SOLUBLE EN ACIDO HIDROTRATADO PARA EL PROCESO DE ALQUILACION. A METHOD FOR THE RECOVERY OF AN ACID CATALYST FROM SOLUBLE OIL IN ACID IS PRESENTED. IT IS FORMED IN A PROCESS FOR THE RENTAL OF HYDROCARBONS AND CONTAINS VALUABLE AMOUNTS OF A SOLD OUT ACID CATALYST, INCLUDING THE ACID TREATMENT: WITH HYDROGEN IN THE PRESENCE OF A CATALYST THAT INCLUDES ONE OR MORE METALS CHOSEN AMONG GROUP VIII OF THE PERIODIC TABLE SUPPORTED IN AN ACID-RESISTANT CARRIER; AND THE TREATMENT OF SOLUBLE OIL IN HYDROTREATED ACID FOR THE RENTAL PROCESS.

一种微丝接触反应器和一种烷基化反应方法

本发明提供了一种微丝接触反应器，包括垂直设置的第一筒体和水平设置的第二筒体，第一筒体的底部为密封，第一筒体内沿纵向间隔设置有多根管道，管道内沿纵向设置有微丝束，管道密封穿过第一筒体的底部和第二筒体的上壁并向下延伸至第二筒体的内部空间中，管道的下端具有开口将第二筒体的内部空间与管道的内部空间连通，第一筒体上设置有物料入口、冷却介质入口和冷却介质出口，物料入口的设置位置使得物料能够进入管道中，冷却介质入口的设置位置使得冷却介质能够进入管道之间的空间，第二筒体上设置有至少一个物料出口。本发明还提供了使用该反应器的烷基化反应方法，该方法极大地降低了液体酸的消耗量和操作能耗。

一种异构烷烃与烯烃的烷基化方法及其装置

本发明涉及异构烷烃与烯烃的烷基化技术领域，特别涉及一种异构烷烃与烯烃的烷基化方法及其装置。该烷基化方法步骤为：异构烷烃和烯烃在催化剂的作用下，在微反应器组中反应，微反应器的反应条件为：反应温度40-200℃，反应压力1.5-4.5MPa；将反应产物进行分离，分别得到目标反应产物、未反应的反应物和催化剂；未反应的反应物和催化剂重新进入微反应器中。提供的设备实现连续化生产，使得烷基化反应快速，时间大大缩短，提高了设备的安全性和反应过程的选择性，避免副反应的发生；整个过程无废物产生，节约成本，防止污染；此外，由于微反应器可以并联多个，可控制同时反应，省略了扩大反应规模的研发开支，进一步节约了成本。

Method for altering an operation of an alkylation unit

One exemplary embodiment can be a method for altering an operation of an alkylation unit during a process upset. The method may include blocking an outlet of a settler to a separation zone, and recycling at least a portion of a hydrocarbon stream to the separation zone to prevent an uncontrolled pressure rise in one or more distillation columns during shutdown of an alkylation reactor.

Method of alkylating paraffins

FIELD: chemistry. ^ SUBSTANCE: invention relates to versions of alkylating isobutene with olefins. One of the versions involves a method of alkylating isobutane with C4 olefin or C4 olefin and at last one of C3 or C5 olefin, involving: (a) feeding isobutene, isopentane and C4 olefin or C4 olefin and at least one of C3 or C5 olefin into a first alkylation system, where a portion of isobutane reacts with a portion of olefin to obtain an output stream which contains a diluted stream of alkylate which contains unreacted components, including isopentane and isobutane; (b) feeding the output stream from the first alkylation system into a debutaniser, where C4 and at least a portion of isopentane are removed as first distillates, and the first alkylation product is removed as first stillage residue; (c) feeding first distillates and a stream containing isobutene into a second alkylation system where isobutane reacts with C4 olefins in said first distillates to form a second alkylation product. ^ EFFECT: use of said methods lowers cost and power consumption owing to a new processing scheme. ^ 39 cl, 3 tbl, 5 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 412 142 (13) C2 (51) МПК C07C 2/56 (2006.01) C07C 11/02 (2006.01) C07C 2/62 (2006.01) C07C 7/04 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2008144399/04, 20.03.2007 (24) Дата начала отсчета срока действия патента: 20.03.2007 (72) Автор(ы): КРОСС Уилльям М. Мл. (US), СМИТ Лоренс А. Мл. (US) R U (73) Патентообладатель(и): КАТАЛИТИК ДИСТИЛЛЕЙШН ТЕКНОЛОДЖИЗ (US) Приоритет(ы): (30) Конвенционный приоритет: 11.04.2006 US 11/402,079 (43) Дата публикации заявки: 20.05.2010 Бюл. № 14 2 4 1 2 1 4 2 (45) Опубликовано: 20.02.2011 Бюл. № 5 (56) Список документов, цитированных в отчете о поиске: US 3236912 А, 22.02.1966. RU 2189373 С2, 20.09.2002. RU 94037755 А1, 10.09.1996. RU 96118230 А, 20.11.1998. 2 4 1 2 1 4 2 R U (86) Заявка PCT: US 2007/ ...

异构烷烃与烯烃的烷基化方法

异构烷烃与烯烃的烷基化方法包括将异构烷烃和烯烃与催化剂接触，所述催化剂为负载型化学表达式为H k YW m Mo 12-m O 40 ·nH 2 O的杂多酸催化剂。其中，k为3或4，Y选自磷、硅、锗或砷原子；m是0～12的正整数；n取大于0至10的任意数；接触反应的温度为异构烷烃的临界温度至300℃，接触反应的压力不低于异构烷烃的临界压力。该方法具有烯烃转化率和烷基化油收率高的优点，同时可保持催化剂的活性稳定性。

烷基化反应装置、反应系统和液体酸催化的烷基化反应方法

一种烷基化反应装置，其特征在于包括n个反应器，所述的n个反应器中，设置有3个反应区的反应器为包括第一反应器在内的m个反应器，以烷基化反应物料流向顺序，所述的3个反应区分别为x反应区、y反应区、z反应区，以混合强度计，y反应区＞x反应区＞z反应区，其中，n≥1且n≥m。

Liquid-phase olefin alkylation process

FIELD: petrochemical synthesis. SUBSTANCE: alkylation of olefin having at least 3 carbon atoms with isoalkane having at least 4 carbon atoms in presence of (i) Lewis acid-based complex catalyst is distinguished by that complex catalyst is product of reaction of at least Lewis acid with general formula R(m-2-z)MX(2+z) wherein M is 3a, 5a, or 5b group metal, X halide, R is C 4 -C 12 -hydrocarbyl, m integer equal to highest oxidation degree of M, Z is equal to 1, 2 or m-2; (ii) hydrogen halide; and (iii) organic compound with up to 12 carbon atoms. EFFECT: simplified process. 15 cl, 4 dwg, 2 tbl, 13 ex УЗ Гс ПЫ ГЭ РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (19) (51) МПК ВИ “” 2438 471 Сл С 07С 2/58, В 01 4 31/22 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 94039538/04, 13.12.1993 (30) Приоритет: 21.12.1992 1$ 07/993,601 19.07.1993 1$ 08093,463 19.07.1993 4$ 08094,520 (46) Дата публикации: 21.09.1999 (56) Ссылки: 4$ 3873635 А, 25.03.75. ЗЦ 400075 А, 03.10.73. $Ц 1172916 А, 08.07.93. (86) Заявка РСТ: Ц$ 93/12087 (13.12.93) (87) Публикация РСТ: \/О 94/14734 (07.07.94) (98) Адрес для переписки: 103735, Москва, ул.Ильинка 5/2, Союзпатент, Патентному поверенному Лебедевой Н.Г. (71) Заявитель: Керр-МакДжи Корпорейшн (ЦЗ) (72) Изобретатель: Ларри Г.Шерман (13), Уилльям А.Юйлл (ЦЗ) (73) Патентообладатель: Керр-МакДжи Корпорейшн (ЦЗ) (54) СПОСОБ ЖИДКОФАЗНОГО АЛКИЛИРОВАНИЯ ОЛЕФИНА (57) Реферат: Описывается способ алкилирования олефина, имеющего по меньшей мере 3 атома углерода, изоалканом, имеющим по меньшей мере 4 атома углерода, в присутствии углеводородного комплексного катализатора на основе кислоты Льюиса, отличающийся тем, что — используют комплексный катализатор, включающий продукт реакции по меньшей мере кислоты Льюиса К(т-2-2)МХ(2+2), где М - металл групп За, 5а или 5в Периодической системы элементов; Х - галогенид; К - гидрокарбильный радикал, имеющий от 1 до 12 атомов углерода; т - целое число, равное наибольшей степени окисления М ...

탄화수소의 촉매 알킬화 방법

자연 순환 반응 및 순환 시스템내 설포란 및 플루오르화수소산 촉매의 존재하에서 알킬화가능한 탄화수소를 반응시키는 알킬화 방법.

Catalyst for alkylating isobutane with c4-olefins and method of producing alkylate

A novel hydrocarbon alkylation catalyst is disclosed comprising a mineral acid and an ether component. A process for utilizing the novel catalyst is also disclosed.

Novel motor fuel alklylation catalyst and process for the use thereof

내용 없음. No content.

Method of alkylation of olefinic hydrocarbons using a catalytic mixture

FIELD: chemical technology. SUBSTANCE: invention relates to a method of alkylation of olefinic hydrocarbons with isoparaffinic hydrocarbons using a mixture of sulfolane and hydrogen fluoride as an alkylation reaction catalyst. Method provides water removing from an alkylation reaction catalyst that is accumulated in alkylation system as a result of water feeding with components of a catalytic mixture. EFFECT: improved method of alkylation. 8 cl, 1 dwg, 1 tbl, 1 ex губе ггс пы ГЭ РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (19) ВИ” 2119 471 ' (51) МПК 13) Сл С 07С 2/62 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 94014626/04, 25.04.1994 (30) Приоритет: 26.04.1993 Ц$ 08051,916 (46) Дата публикации: 27.09.1998 (56) Ссылки: Ц$ 5191150 А, 02.03.93. ЗЦ 977444 А, 30.11.82. ОЕ 1418433 АЛ, 09.07.10. (71) Заявитель: Филипс Петролеум Компани (Ц$) (72) Изобретатель: Ричард Ли Андерсон (Ц$) (73) Патентообладатель: Филипс Петролеум Компани (1$) (54) СПОСОБ АЛКИЛИРОВАНИЯ ОЛЕФИНОВЫХ УГЛЕВОДОРОДОВ С ИСПОЛЬЗОВАНИЕМ КАТАЛИТИЧЕСКОЙ СМЕСИ (57) Реферат: Раскрывается способ алкилирования олефиновых углеводородов изопарафиновыми углеводородами, В котором используется В качестве катализатора алкилирования смесь сульфолана и — Фторводорода. — Способ обеспечивает удаление воды из катализатора алкилирования, которая накапливается в системе алкилирования в результате поступления воды с компонентами, составляющими каталитическую смесь. 7 з.п.ф-лы, 1 ил., 1 табл. 2119471 С1 КО губе ггс пы ГЭ КУЗЗАМ АСЕМСУ ГОК РАТЕМТ$ АМО ТКАОЕМАКК$ (19) ВИ” 2119 471 ' 13) СЛ (51) 1пЕ. С1.6 С 07 с 262 12) АВЗТКАСТ ОЕ 1МУЕМТОМ (21), (22) АррИсаНоп: 94014626/04, 25.04.1994 (30) Рпошу: 26.04.1993 Ц$ 08/051,916 (46) Рае ог ричбИсанНоп: 21.09.1998 (71) АррИсапе: ЕИрз Регоеит Котрап! (Ц$) (72) пуетщог. — Еспага Ш Апаегзоп (4$) (73) Ргорпеюг: -Ир$ Регоеит Котрап! (0$) (54) МЕТНОО ОР АЕКУЕАТЮОМ ОЕ ОГЕНМС НУОКОСАКВОМ$ ЦЗМС А САТАЁЕУТ!С МХТОУВЕ (57) АБзГасЕ: НЕЕО: спегтлсеа! 1есйптоюду. ...

Способ регенерации отработанного кислотного катализатора

Объектом изобретения является способ регенерации отработанного кислотного катализатора, используемого для алкилирования углеводородов, включающий обработку реагентом жидкой фазы, при этом обработку осуществляют путем экстрагирования водой, упаривания полученного водного экстракта и этерификации полученного остатка содержащим олефин потоком углеводорода, причем в качестве жидкой фазы обработке подвергают масло, образующееся в качестве побочного продукта во время процесса алкилирования.

Alkylation by controlling olefin ratios

Disclosed are various embodiments for alkylating olefins and isoparaffins in the presence of an acid to reduce and/or control acid consumption or maximize and/or control the octane number of the produced alkylate product. One embodiment includes alkylation by controlling the C 3 /iso-C 5 olefin ratio to reduce acid consumption. Another embodiment includes alkylation of C 3 and C 5 olefins in separate alkylation zones to maximize alkylate octane number. Even another embodiment includes propylene alkylation followed by C 4 and/or C 5 olefin alkylation, with the spent propylene acid used in the C 4 and/or C 5 olefin alkylation. Still another embodiment includes alkylation of C 3 , C 4 and C 5 olefins in separate alkylation zones, with the spent propylene acid used in the C 4 alkylation, and the spent butylene acid used in the C 5 alkylation. Yet another embodiment includes alkylation by controlling the C 3 /C 4 olefin ratio to maximize the octane number of the produced alkylate.

Solid aliphatic alkylation catalyst

The invention concerns a catalyst comprising a porous organic or inorganic support and at least one active phase comprising at least one acid selected from acids with formula R--SO 3 H, where R is fluorine or an alkyl group or a fluorinated alkyl group, and at least one weakly basic aprotic organic solvent, the support having been impregnated with the active phase, the catalyst being such that it is essentially constituted by particles with an average diameter in the range 0.1 μm to 150 μm, and being such that before impregnation with the active phase, the support has a total pore volume in the range 0.5 cm 3 /g to 6 cm 3 /g. The invention also concerns the use of the catalyst for aliphatic alkylation.

Solid catalysts based on fluorinated graphite

A process and a catalyst composition to effect hydrocarbon transformations comprising contacting a hydrocarbon charge with a catalyst comprising a fluorinated graphite having a fluorine to carbon atomic ratio of from about 0.1 to 1 and having bonded thereto from about 5 to 50 percent by weight of the total weight of the catalyst of at least one Lewis acid compound selected from halides of the elements of Group IIA, IIIA, IVB, V or VIB of the Periodic Table. In addition, the catalysts may also have bonded thereto a minor portion of a Bronsted acid and/or a metal of Group IVB or VIII of the Periodic Table.

Use of a catalyst for paraffins alkylation

Catalyst based on silica and sulphuric acid and its use in catalytic alkylation of isobutane and/or isopentane in the presence of at least one olefin containing from 3 to 6 carbon atoms per molecule.

Environmentally safe alkylation of aliphatic and aromatic hydrocarbons with olefins using solid HF-equivalent catalysts

Solid polymeric onium poly(hydrogen fluoride) complexes disclosed herein can be used for alkylating aliphatic or aromatic hydrocarbons with olefins. These solid polymeric complexes can be formed by a process of contacting a source of hydrogen fluoride with a homopolymer or copolymer containing in at least one repeat unit, a nitrogen, phosphorus, or sulfur atom, capable of forming an onium fluoride moiety upon reaction or complexation with the hydrogen fluoride source.

Supported superacidic catalysts based on C10 to C18 perfluorinated alkanesulfonic acids

The present invention relates to supported superacidic catalysts comprising C 4 -C 18 , preferentially C 6 to C 12 , perfluorinated alkanesulfonic acid absorbed on suitable supports, such as fluorinated alumina, alumina silica and other chalcides having bonded thereto subsequently a Lewis acid compound selected from the higher valency fluorides of the elements of Groups IIA, IIIA, IVB, VA or VIB of the Periodic Table. The invention includes a process for catalytic transformation of hydrocarbons.

Supported heteropoly acid catalysts for isoparaffin-olefin alkylation reactions

The alkylation of isoparaffin with olefin to provide alkylate is carried out in the presence of, as catalyst, a supported heteropoly acid. The support may be MCM-41, and the heteropoly acid may be dodecawolframophosphoric acid (i.e., phosphotungstic acid, i.e., H3PW12O40).

Supported heteropoly acid catalysts

There is provided a catalyst comprising a heteropoly acid, such as phosphotungstic acid, supported on a mesoporous crystalline material, such as M41S. A particular form of this M41S support is designated as MCM-41. There is also provided a method for preparing this catalyst by impregnating the heteropoly acid on the support. There is also provided a process for using this catalyst to catalyze acid catalyzed reactions, such as the isomerization of paraffins and the alkylation of aromatics.

Environmentally safe alkylation of aliphatic and aromatic hydrocarbons with olefins using solid HF-equivalent catalysts

A method of alkylating aliphatic or aromatic hydrocarbons with olefins using solid hydrogen fluoride-equivalent catalysts is described. Preferred catalysts comprise solid polymeric onium polyhydrogen fluoride complexes.

SOLID ALIPHATIC ALKYLATION CATALYST

Process for the alkylation of aliphatic hydrocarbons with olefins

A process for the alkylation of aliphatic hydrocarbons with olefins catalyzed by a silica-based material, characterised in that the surface Si-OH groups of said silica are esterified with a fluoroalkylsulphonic acid of formula CF₃(CF₂) n SO₃H, where n is a whole number between 0 and 11, said material having a Hammett acidity H O ≦ -11.4.

HF alkylation process with internal acid regeneration

An improved process for removing polymeric by-product (ASO) from the HF alkylation acid in an HF alkylation unit used for the production of gasoline boiling range alkylate product by olefin/iso-paraffin alkylation, comprises fractionating a portion of the circulating HF alkylation acid inventory of the unit with a portion of hot alkylate product in a fractionation zone to from an overhead product comprising HF alkylation acid and water and a bottoms fraction comprising the polymeric by-product and alkylate. The bottoms fraction is sent to the isoparaffin stripper of the unit to remove trace HF alkylation acid as overhead and form a product stream of hot alkylate as a bottoms fraction.

Method of regeneration of catalyst for alkylation of isoparaffins by olefins

FIELD: catalysts for organic syntheses. SUBSTANCE: invention relates to a method of regeneration of alkylation catalyst containing sulfone group and a method of removing regenerating agent from catalyst. Method is distinguished by that sulfone group containing substance is sulfolane and material adsorbing regenerating agent is selected from the group containing aluminum oxide, carbon, and their mixtures. EFFECT: facilitated regeneration. 12 cl, 2 dwg, 3 tbl с 90сО0гс пы Го РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (19) (51) МПК ВИ "” 2 103 063 ' В 01 3 27/32, 31/40, С 07 С 2/20 13) СЛ 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 93050201/04, 24.06.1993 (30) Приоритет: 26.06.1992 Ц$ 07/904938 (46) Дата публикации: 27.01.1998 (56) Ссылки: ЕР, патент, 0184375, кл. С 10С 532, 1985. (71) Заявитель: Филлипс Петролеум Компани (Ц$) (72) Изобретатель: Рональд Гордон Аббот [ЦЗ], Алан Дэн Истмэн[Ц$] (73) Патентообладатель: Филлипс Петролеум Компани (1$) (54) СПОСОБ РЕГЕНЕРАЦИИ КАТАЛИЗАТОРА АЛКИЛИРОВАНИЯ ИЗОПАРАФИНОВ ОЛЕФИНАМИ (57) Реферат: Изобретение относится к новому способу регенерирования катализатора алкилирования, который содержит компонент сульфона и способ удаления КРМ из катализатора — алкилирования, причем указанный сульфон является сульфоланом, а КРМ-адсорбирующий материал, выбранный из группы, состоящей их оксида алюминия, углерода и их смесей. 11 з.п. ф-лы, 3 табл., 2 ил. „=“ фиг.1 2103063 С1 КО с 90сО0гс пы ГЭ (19) 13) ВИ “” 2 403 063 ^^ Сл (51) 216 В 04 4] 27/32, 31/40, С 07 С 2/20 КУЗЗАМ АСЕМСУ ГОК РАТЕМТ$ АМО ТКАОЕМАКК$ 12) АВЗТКАСТ ОЕ 1МУЕМТОМ (21), (22) АррИсаНоп: 93050201/04, 24.06.1993 (71) АррИсапе: ЕИйрз Регаеит Котрап! (ЦЗ) (30) Рношу: 26.06.1992 Ц$ 07/904938 (72) пуетщог. — КопаГа Согаоп АББо ИЗ], (46) Бае ог ричбИсанНоп: 27.01.1998 А!ап Оейп 15тевп[4$] (73) Ргорпеюг: ЕИр$ Регоеит Котрап! (Ц$) (54) МЕТНОО ОЕ КЕСЕМЕКАТЮМ ОЕ САТАЕУЗТ РОК АЕКУГАТЮОМ ОЕ 1ЗОРАКАРЕМ$ ВУ ОГЕНМЗ$ (57) АБзГасЕ: НЕГО: саау$$ ог огдатс ...