CN1286782C - Method for isomerization of light hydrocarbon - Google Patents
Method for isomerization of light hydrocarbon Download PDFInfo
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- CN1286782C CN1286782C CN 03102218 CN03102218A CN1286782C CN 1286782 C CN1286782 C CN 1286782C CN 03102218 CN03102218 CN 03102218 CN 03102218 A CN03102218 A CN 03102218A CN 1286782 C CN1286782 C CN 1286782C
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Abstract
The present invention relates to a method for the isomerization of light hydrocarbon. In the method, a raw material of light hydrocarbon is isomerized in a front isomerization reactor first; after gas-liquid separation is carried out on a material flow from an output of the front reactor, the obtained liquid material flow is separated in an isomerized alkane eliminating tower; a tower top material flow using isomerized alkane as a main component is used as an isomerized product and is fed in a gasoline stabilization system; a tower bottom material flow using normal alkane as a main component is introduced into a rear isomerization reactor; after gas-liquid separation is carried out on a reaction material flow of the rear isomerization reactor, one part of a material flow is used as an isomerized product to be fed in the gasoline stabilization system, and the other part of the liquid phase material flow returns back and is used as a feeding material of the isomerized alkane eliminating tower. In the method, after isomerized alkane is eliminated from a front isomerization reaction product, the separated normal alkane is further isomerized in the rear isomerization reactor, the isomerization conversion rate of the normal alkane is improved, and an octane value of a raw material of light hydrocarbon is increased to a great extent.
Description
Technical field
The present invention relates to a kind ofly prepare the method for hydrocarbon from the hydrocarbon that contains same carbon atoms number, more particularly, is that a kind of straight-chain paraffin that carbonatoms is less generates branched isoparaffin by isomerization reaction, to improve the method for light hydrocarbon feedstocks octane value.
Background technology
In the time processing and secondary processing process of crude oil, can produce with C5, C6 is the main light ends fractionation of forming, this light ends fractionation can be used as the raw material of blend component, cracking of ethylene raw material or the lighter hydrocarbons producing hydrogen from steam conversion of gasoline, the economic benefit maximum of bringing to enterprise as the blend component of gasoline wherein, but, its mediation quantity in gasoline is restricted because the normal paraffin in the lighter hydrocarbons has lower octane value.If the normal paraffin in the lighter hydrocarbons is converted into isoparaffin, the octane value of lighter hydrocarbons will be effectively improved, and can increase the mediation quantity of lighter hydrocarbons in the gasoline, and this can alleviate alkene and the too high problem of aromaticity content in China's gasoline to a certain extent.
The exploitation of light hydrocarbon isomerization technology and industrial application are the bases that is developed as with isomerization catalyst.One of isomerization method for light hydrocarbon commonly used is to carry out hydroisomerization reaction more than 250 ℃ with the difunctional isomerization catalyst of zeolite type, described zeolite type dual-function catalyst mainly is meant with the crystalline silicate to be carrier, aluminum oxide and other refractory oxide are binding agent, supported V III family metal, it mainly is the catalyzer of platinum or palladium preparation, used carrier mainly contains X type zeolite, y-type zeolite and mordenite at present, because mordenite has good high-temperature stability, therefore be that the isomerization catalyst of preparing carriers has obtained development rapidly with the mordenite.But because the zeolite type dual-function catalyst is to lean on the acidity of carrier to promote the normal alkane isomerization reaction, activity of such catalysts is lower, needs higher temperature of reaction.USP4,789,655 introduce chlorine by the gas phase oxi-chlorination in the mordenite catalyst that carries platinum, and making cl content is the catalyzer of 0.5～10 heavy %.USP3,932,554 adopt fluorine-containing halon to contact with the mordenite catalyst that carries platinum or palladium, make the modified catalyst that fluorine content is at least 0.86 heavy %.Owing in carrier, introduced chlorine and fluorine element, improved the acidity of catalyzer, the isomerization performance of catalyzer is improved, but in the use of catalyzer, chlorine or fluorine can run off gradually along with the carrying out of reaction, cause catalyst activity reduction, and device is corroded.In recent years, the β zeolite is applied in the carrier of catalyst for isomerizing light hydrocarbon, and as USP5,095,169 to disclose a kind of be the isomerization catalyst of preparing carriers with activatory β zeolite, and this catalyzer has had raising to a certain degree aspect selectivity.
At present, light hydrocarbon isomerization technology can be divided into two types, and promptly raw material is once by type and part normal paraffin circular form.Raw material once by the isomerization process of type is, light hydrocarbon feedstocks is once by isomerization reactor, isomerization product through after stable promptly as product.As USP4,804,803 isomerization methods of mentioning, C5 with the C6 hydrocarbon with after hydrogen mixes through two placed in-line isomerization reactors, the following hydro carbons of separating isomerism product and C4 in stabilizer tower then.The isomerization process of part normal paraffin cyclical patterns is, isomerization reaction product is separated isoparaffin wherein by suitable separation means with normal paraffin, then, again part or all of normal paraffin is delivered to the inlet of reactor, realize the circulation of normal paraffin in reactive system, improve the transformation efficiency of normal paraffin.As USP4,831, the light hydrocarbon isomerization technology of mentioning in 209, C5, the C6 paraffinic feedstock is through isomerization reactor, behind gas-liquid separator and the preflash tower, enter and take off the isohexane tower, the positive structure C6 alkane of separating draws the inlet that is back to reactor, but this method is owing to enter reactor once more after returning material and raw material mixing, be implemented in the circulation in the reactive system, the isoparaffin that contains in the raw material can suppress the isomerization reaction of normal paraffin, to further improve the transformation efficiency of normal paraffin, have only the flow that returns material by increase, thereby cause the increase of plant energy consumption.USP5,233,120 and USP5, in the light hydrocarbon isomerization technology of mentioning in 602,291, isomerization reaction product has been carried out the selective adsorption separation, normal paraffin wherein is back to the inlet of reactor, normal paraffin almost can reach whole conversions, and the octane value of light hydrocarbon feedstocks is greatly improved, but the equipment of adsorption process and operate equal more complicated.
Because the light hydrocarbon isomerization reaction is controlled by thermodynamic(al)equilibrium, under specific temperature of reaction and pressure condition, the transformation efficiency of normal paraffin is certain in the raw material.Therefore, improve the transformation efficiency of normal paraffin, need to change the residing condition of isomerization reaction, one of method of employing is suitably to reduce temperature of reaction, but under the specific catalyst condition, the reduction of temperature of reaction is subjected to the restriction of speed of response; Two of the method that adopts is that the normal paraffin in the isomerization reaction product is separated with isoparaffin, and partly or entirely the inlet of normal paraffin Returning reactor carries out further isomerization reaction.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of thereby normal paraffin in the raw material is converted into the isomerization method for light hydrocarbon that isoparaffin improves the raw material octane value greatly with higher transformation efficiency.
Method provided by the invention comprises: isomerization reaction forwardly takes place in the isomerization reactor earlier in light hydrocarbon feedstocks, and the temperature of reaction in the anterior isomerization reactor is 100～400 ℃, and reaction pressure is 0.5～5.0MPa, and raw material feed weight air speed is 0.2～10.0h
-1Hydrogen/oil mol ratio is 0.05～5.0, the outlet logistics of anterior reactor is after gas-liquid separation, the gained liquid phase stream separates in taking off the isoparaffin tower, is the main overhead stream of forming with the isoparaffin, goes the gasoline stable system as isomerization product, with the normal paraffin is that the main tower base stream of forming is introduced in the rear portion isomerization reactor, temperature of reaction in the isomerization reactor of rear portion is 100～400 ℃, and reaction pressure is 0.5～5.0MPa, and raw material feed weight air speed is 0.2～10.0h
-1Hydrogen/oil mol ratio is 0.05～5.0, the reactant flow of rear portion isomerization reactor is after gas-liquid separation, part liquid phase stream goes the gasoline stable system as isomerization product, another part liquid phase stream returns and as the charging of taking off the isoparaffin tower, described light hydrocarbon feedstocks is a kind of or its mixture in C4～C7 hydro carbons.
Method provided by the invention is separated the reaction product of anterior isomerization reactor in taking off the isoparaffin tower, normal paraffin wherein carries out further isomerization reaction in the isomerization reactor of rear portion, improved the isomerisation conversion of normal paraffin, the octane value of light hydrocarbon feedstocks has had raising by a relatively large margin.
Description of drawings
Accompanying drawing is an isomerization method for light hydrocarbon synoptic diagram provided by the invention.
Embodiment
The present invention is so concrete enforcement:
Two portions before and after the light hydrocarbon isomerization reactive system is divided into, the raw material of anterior reactive system is a kind of or its mixture in the preferred C5 of C4～C7～C6 hydro carbons, this raw material is based on various alkane, come from normal pressure tops, hydrogenation unit light naphthar, reformer light naphthar etc., boiling point is lower than 80 ℃, and the raw material of rear portion reactive system is to be the main lighter hydrocarbons of forming with the normal paraffin.
With various alkane serves as that the main light hydrocarbon isomerization raw material of forming mixes with recycle hydrogen after the fresh feed pump supercharging, mixture passes through the feed exchanger heat exchange respectively, the heating of charging process furnace, reach the reaction temperature required after, enter anterior isomerization reactor, the isomerization reaction of normal paraffin forwardly takes place in the isomerization reactor, the reactor outlet logistics is respectively through heat exchange, after the cooling, enter gas-liquid separator, in gas-liquid separator, realize the separation of gas-liquid two-phase, wherein gas phase is main the composition with hydrogen, mix with the recycle hydrogen of rear portion reactive system, and be delivered to recycle compressor by pipeline, after the recycle compressor supercharging, the inlet of delivering to reactor with the new hydrogen that replenishes recycles; The liquid phase of gas-liquid separator is mixed with the return logistics of rear portion reactive system, after the interchanger heat exchange, enters and takes off the isoparaffin tower.
The reactant flow of anterior reactive system and the return logistics of rear portion reactive system separate in taking off the isoparaffin tower, are the main cat head liquid phase of forming with the isoparaffin, go the gasoline stable system as isomerization product.Be that liquid phase is mixed with recycle hydrogen at the bottom of the main tower of forming with the normal paraffin, heat through process furnace, after reaching the required temperature of reaction, enter the rear portion isomerization reactor, the reactor outlet logistics enters gas-liquid separator after heat exchange, cooling, the gas phase of gas-liquid separator is delivered to the inlet of recycle compressor, the liquid phase part of gas-liquid separator is circulated to takes off isoparaffin tower forward heat exchanger entrance, a part as isomerization product with go the gasoline stable system after the liquid phase stream that takes off the isoparaffin cat head mixes; The amount of returning of gas-liquid separator liquid phase can be regulated as required, in addition, also can not establish return logistics, and whole liquid phases of rear portion gas-liquid separator are gone the gasoline stable system as isomerization product.Anterior, rear portion isomerization reactor outlet logistics can a shared gas-liquid separator, also can distinguish each with a gas-liquid separator.
Anterior isomerization reactor and rear portion isomerization reactor can be a plurality of reactors in series, and the number of reactors that is adopted is generally 1～2 reactor.When adopting a plurality of reactors in series, the general lower circulation gas of temperature that between two adjacent reactors, replenishes, the so just overall temperature rise of controlling reactor effectively, and the temperature that can regulate next reactor inlet logistics helps improving the transformation efficiency of normal paraffin.
Anterior isomerization reactor and rear portion isomerization reactor can adopt identical reaction conditions, also can adopt different reaction conditionss, but the scope of reaction conditions is identical, promptly be respectively: 100～400 ℃ preferred 230～300 ℃ of temperature, preferred 1.0～the 3.0MPa of pressure 0.5～5.0MPa, raw material feed weight air speed 0.2～10.0h
-1Preferred 0.5～3.0h
-1, hydrogen/oil mol ratio is 0.05～5.0 preferred 0.1～3.0.
In anterior isomerization reactor and the rear portion isomerization reactor isomerization catalyst is housed all, described isomerization catalyst is made up of VIII family metal and the carrier of 0.01～3.0 heavy %.VIII family metal in the catalyzer can be platinum, palladium, germanium, ruthenium, rhodium etc.; The carrier of catalyzer can be a mordenite, wherein contains a certain amount of halogen, also can be the complex carrier that aluminum oxide and mordenite are formed, and can also further contain the β zeolite in this complex carrier.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed, but does not therefore limit present method.
Accompanying drawing is an isomerization method for light hydrocarbon synoptic diagram provided by the invention.
Isomerization method for light hydrocarbon flow process provided by the invention is as follows: the light hydrocarbon isomerization raw material is through pipeline 1 introducing device, after pump 2 superchargings, enter pipeline 3, mix with recycle hydrogen from pipeline 60, enter pipeline 4, then pass through feed exchanger 5 successively, pipeline 6, charging process furnace 7, pipeline 8, reach reactor inlet temperature required after, enter anterior reactor 9, chemical reaction based on normal alkane isomerization takes place in reactor 9, reaction product is successively via pipeline 10, feed exchanger 5, pipeline 11, air-cooler 12, pipeline 13, water cooler 14 and pipeline 15 enter the separation that gas-liquid separator 16 is finished gas-liquid two-phase.
The gas phase of gas-liquid separator 16 is based on hydrogen, this gas phase is drawn through pipeline 53, after mixing from the gas phase of pipeline 54, enter recycle compressor 56 through pipeline 55, gas phase after the supercharging through pipeline 57 with enter pipeline 59 after the new hydrogen that replenishes through pipeline 58 mixes, gas phases in the pipeline 59 are divided into two strands, and wherein a stock-traders' know-how pipeline 60 mixes with light hydrocarbon isomerization raw material from pipeline 3, and another strand is then through pipeline 61 and from the liquid mixing of pipeline 24.
The liquid phase of gas-liquid separator 16 is drawn through pipeline 17, after liquid-phase mixing from pipeline 37, successively through pipeline 18, interchanger 19, pipeline 20 enters and takes off isoparaffin tower 21, the effect of taking off the isoparaffin tower is that the isoparaffin component in the isomerization reaction product is separated with normal paraffin component, with the isoparaffin is that the main cat head gas phase of forming is drawn through pipeline 42, successively through air-cooler 43, pipeline 44, watercooler 45 and pipeline 46, enter return tank of top of the tower 47, the gas phase of return tank 47 enters the fuel gas pipe network by pipeline 52, the liquid phase of return tank 47 is then drawn through pipeline 48, after pump 49 superchargings, a part is returned cat head through pipeline 50, and another part is then drawn the gasoline stable system through pipeline 51.Take off in the isoparaffin tower bottom material one successively through pipeline 39, reboiler 40 and pipeline 41 return at the bottom of the tower, for the operation of taking off the isoparaffin tower provides thermal source, another strand material is then drawn through pipeline 22 at the bottom of the tower, after pump 23 superchargings, be mixed and fed into pipeline 25 with recycle hydrogen from pipeline 61, after charging process furnace 26 is heated to the required temperature of reactor inlet, enter reactor 28 through pipeline 27, in reactor 28, further carry out the isomerization reaction of normal paraffin, reactant flow is drawn through pipeline 29, pass through interchanger 19 successively, pipeline 30, air-cooler 31, pipeline 32, watercooler 33 and pipeline 34 enter gas-liquid separator 35.
The gas phase of gas-liquid separator 35 is drawn through pipeline 54 and is delivered to recycle compressor, and the liquid phase of gas-liquid separator 35 is then drawn through pipeline 36, and a part is through the charging that pipeline 37 returns and the isoparaffin tower is taken off in conduct, and another part is then drawn the gasoline stable system through pipeline 38.
Method advantage provided by the invention is:
1, in isomerization method for light hydrocarbon of the present invention, the reaction product of anterior isomerization reactor is separated in taking off the isoparaffin tower, normal paraffin wherein carries out further isomerization reaction in the isomerization reactor of rear portion, improved the isomerisation conversion of normal paraffin, the octane value of light hydrocarbon feedstocks has had raising by a relatively large margin.
2, after the reaction product of rear portion isomerization reactor is carried out gas-liquid separation in the gas-liquid separator of rear portion, part liquid-phase product is back to and takes off the isoparaffin tower, mix with the liquid-phase product of anterior reactor, as the charging of taking off the isoparaffin tower, realize the circulation of part normal paraffin in the reactive system of rear portion, further improved the isomerisation conversion of normal paraffin.
3, the present invention is except that being applicable to new device, and also being specially adapted to idle catalytic reforming unit is the isomerization unit that transform on the basis, and the rate that reuses of device is very high, needs to increase newly equipment hardly.
4, the shared recycle compressor of anterior isomerization reaction system and rear portion isomerization reaction system helps saving facility investment and energy consumption.
The following examples will give further instruction to present method, but therefore not limit present method.
The used catalyzer trade mark is FI-15 in embodiment and the Comparative Examples, is produced by Fushun petrochemical corporation (complex) catalyst plant.
Present embodiment adopts technical process shown in the drawings, describes from several aspects such as the composition of the composition of light hydrocarbon feedstocks and character, isomerization principal reaction condition and isomerization product and character below:
1. the composition of light hydrocarbon feedstocks and character
The weight of light hydrocarbon feedstocks is composed as follows:
Normal butane, heavy % 2.60
Trimethylmethane, heavy % 0.30
Skellysolve A, heavy % 23.54
Iso-pentane, heavy % 9.56
Pentamethylene, heavy % 1.39
Normal hexane, heavy % 32.66
Isohexane, heavy % 22.13
Hexanaphthene and methylcyclopentane, heavy % 4.15
Benzene, heavy % 1.65
C7 and above hydro carbons, heavy % 2.03
Light hydrocarbon feedstocks is if the research octane number (RON) after gasoline stabilizer removes light constituent should be 59.4, and its octane value is very low.Since at present to the OR Octane Requirements of gasoline products all than higher, generally all more than 90, if light hydrocarbon feedstocks is handled without suitable means, just directly call in the gasoline products, will influence the quality of gasoline products, therefore, light hydrocarbon feedstocks is carried out isomerization handle, it is necessary improving its octane value.
2. isomerization principal reaction condition
The temperature in of anterior reactor, ℃ 250
The inlet pressure of anterior reactor, MPa 1.95
Charging is the interior weight hourly space velocity of reactor forwardly, h
-11.0
Hydrogen/oil mol ratio 2.6 in the anterior reactor
The temperature in of rear portion reactor, ℃ 250
The inlet pressure of rear portion reactor, MPa 1.85
The weight hourly space velocity of charging in the reactor of rear portion, h
-11.0
Hydrogen/oil mol ratio 2.6 in the reactor of rear portion
The circulation ratio of rear portion gas-liquid separator liquid phase stream, heavy % 61.6
3. the composition of isomerization product and character
The weight of isomerization product is composed as follows:
The following alkane of C3, heavy % 3.3
Normal butane, heavy % 3.7
Trimethylmethane, heavy % 0.4
Skellysolve A, heavy % 12.0
Iso-pentane, heavy % 20.8
Pentamethylene, heavy % 1.4
Normal hexane, heavy % 3.1
Isohexane, heavy % 49.0
Hexanaphthene and methylcyclopentane, heavy % 5.4
Benzene, heavy % 0.5
C7 and above hydro carbons, heavy % 0.4
The research octane number (RON) of isomerization product after gasoline stabilizer removes light constituent is 82.4, its research octane number (RON) is compared with the octane value of raw material raising by a relatively large margin, therefore, can suitably improve the harmonic proportion of isomerization product in gasoline products, and then alleviate alkene and the too high problem of aromaticity content in the gasoline products.
Flow process that present embodiment adopted and technical process shown in the drawings are basic identical, and difference is that the liquid phase of rear portion gas-liquid separator is all gone the gasoline stable system as isomerization product, the liquid phase stream that cancellation is returned.Describe from several aspects such as the composition of the composition of light hydrocarbon feedstocks and character, isomerization principal reaction condition and isomerization product and character below:
1. the composition of light hydrocarbon feedstocks and character
The employed light hydrocarbon feedstocks of present embodiment is identical with embodiment 1 employed light hydrocarbon feedstocks.
2. isomerization principal reaction condition
The temperature in of anterior reactor, ℃ 250
The inlet pressure of anterior reactor, MPa 1.95
Charging is the interior weight hourly space velocity of reactor forwardly, h
-11.0
Hydrogen/oil mol ratio 2.6 in the anterior reactor
The temperature in of rear portion reactor, ℃ 250
The inlet pressure of rear portion reactor, MPa 1.85
The weight hourly space velocity of charging in the reactor of rear portion, h
-11.0
Hydrogen/oil mol ratio 2.6 in the reactor of rear portion
The circulation ratio 0 of rear portion gas-liquid separator liquid phase stream
3. the composition of isomerization product and character
The weight of isomerization product is composed as follows:
The following alkane of C3, heavy % 3.1
Normal butane, heavy % 3.7
Trimethylmethane, heavy % 0.4
Skellysolve A, heavy % 12.0
Iso-pentane, heavy % 20.7
Pentamethylene, heavy % 1.4
Normal hexane, heavy % 5.0
Isohexane, heavy % 47.2
Hexanaphthene and methylcyclopentane, heavy % 5.6
Benzene, heavy % 0.5
C7 and above hydro carbons, heavy % 0.4
The research octane number (RON) of isomerization product after gasoline stabilizer removes light constituent is 81.0, and its research octane number (RON) is compared the raising that also has by a relatively large margin with the octane value of raw material.
Comparative Examples 1
In the technical process of this Comparative Examples, light hydrocarbon feedstocks after an isomerization reaction, reaction effluent through gas-liquid separation gained liquid phase promptly as isomerization product, and without taking off isoparaffin and isomerization reaction for the second time.Describe from several aspects such as the composition of the composition of light hydrocarbon feedstocks and character, isomerization principal reaction condition and isomerization product and character below:
1. the composition of light hydrocarbon feedstocks and character
The employed light hydrocarbon feedstocks of this Comparative Examples is identical with embodiment 1 employed light hydrocarbon feedstocks.
2. isomerization principal reaction condition
The temperature in of reactor, ℃ 250
The inlet pressure of reactor, MPa 1.95
The weight hourly space velocity of charging in reactor, h
-11.0
Hydrogen/oil mol ratio 2.6 in the reactor
3. the composition of isomerization product and character
The weight of isomerization product is composed as follows:
The following alkane of C3, heavy % 2.4
Normal butane, heavy % 3.2
Trimethylmethane, heavy % 0.4
Skellysolve A, heavy % 11.4
Iso-pentane, heavy % 19.4
Pentamethylene, heavy % 1.3
Normal hexane, heavy % 10.4
Isohexane, heavy % 44.2
Hexanaphthene and methylcyclopentane, heavy % 6.4
Benzene, heavy % 0.5
C7 and above hydro carbons, heavy % 0.4
The research octane number (RON) of isomerization product after gasoline stabilizer removes light constituent is 77.5, and its research octane number (RON) is compared with the octane value of raw material raising to a certain degree, but compares with embodiment 1 and embodiment 2, and the amplitude that octane value improves is little.
Comparative Examples 2
Flow process of this Comparative Examples and flow process of the present invention difference only are, the former separates and to obtain positive structure C6 alkane and return former reactor inlet and mix with raw material from taking off the isohexane tower, rather than entering another isomerization reactor, the part heavy constituent are discharged at the bottom of by tower and are mixed as isomerization product with the cat head liquid-phase product.
Describe from several aspects such as the composition of the composition of light hydrocarbon feedstocks and character, isomerization principal reaction condition and isomerization product and character below:
1. the composition of light hydrocarbon feedstocks and character
The employed light hydrocarbon feedstocks of this Comparative Examples is identical with embodiment 1 employed light hydrocarbon feedstocks.
2. isomerization principal reaction condition
The temperature in of reactor, ℃ 250
The inlet pressure of reactor, MPa 1.95
The weight hourly space velocity of charging in reactor, h
-11.0
Hydrogen/oil mol ratio 2.6 in the reactor
Liquid phase stream circulation ratio at the bottom of the tower, heavy % 61.6
3. the composition of isomerization product and character
The weight of isomerization product is composed as follows:
The following alkane of C3, heavy % 3.0
Normal butane, heavy % 3.7
Trimethylmethane, heavy % 0.4
Skellysolve A, heavy % 12.1
Iso-pentane, heavy % 20.7
Pentamethylene, heavy % 1.4
Normal hexane, heavy % 5.8
Isohexane, heavy % 46.6
Hexanaphthene and methylcyclopentane, heavy % 5.6
Benzene, heavy % 0.5
C7 and above hydro carbons, heavy % 0.4
The research octane number (RON) of isomerization product after gasoline stabilizer removes light constituent is 80.5, and its research octane number (RON) is compared with the octane value of raw material raising to a certain degree, but compares with embodiment 1 and embodiment 2, and the amplitude that octane value improves is less.
Claims (3)
1, a kind of isomerization method for light hydrocarbon, it is characterized in that light hydrocarbon feedstocks forwardly in the isomerization reactor isomerization reaction takes place earlier, temperature of reaction in the anterior isomerization reactor is 100～400 ℃, and reaction pressure is 0.5～5.0MPa, and raw material feed weight air speed is 0.2～10.0h
-1Hydrogen/oil mol ratio is 0.05～5.0, the outlet logistics of anterior reactor is after gas-liquid separation, the gained liquid phase stream separates in taking off the isoparaffin tower, is the main overhead stream of forming with the isoparaffin, goes the gasoline stable system as isomerization product, with the normal paraffin is that the main tower base stream of forming is introduced in the rear portion isomerization reactor, temperature of reaction in the isomerization reactor of rear portion is 100～400 ℃, and reaction pressure is 0.5～5.0MPa, and raw material feed weight air speed is 0.2～10.0h
-1Hydrogen/oil mol ratio is 0.05～5.0, the reactant flow of rear portion isomerization reactor is after gas-liquid separation, part liquid phase stream goes the gasoline stable system as isomerization product, another part liquid phase stream returns and as the charging of taking off the isoparaffin tower, described light hydrocarbon feedstocks is a kind of or its mixture in C4～C7 hydro carbons.
2,, it is characterized in that described light hydrocarbon feedstocks is a kind of or its mixture in C5～C6 hydro carbons according to the method for claim 1.
3,, it is characterized in that front portion, the rear portion isomerization reactor outlet shared gas-liquid separator of logistics or difference are respectively with a gas-liquid separator according to the method for claim 1.
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|---|---|---|---|
| CN 03102218 CN1286782C (en) | 2003-01-30 | 2003-01-30 | Method for isomerization of light hydrocarbon |
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|---|---|---|---|
| CN 03102218 CN1286782C (en) | 2003-01-30 | 2003-01-30 | Method for isomerization of light hydrocarbon |
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Families Citing this family (4)
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| CN101497815B (en) * | 2008-01-31 | 2012-09-12 | 中国石油化工股份有限公司 | Isomerization method for light hydrocarbon |
| CN101544905B (en) * | 2008-03-27 | 2012-09-12 | 中国石油化工股份有限公司 | Light hydrocarbon isomerization method |
| CN107916131B (en) * | 2016-10-11 | 2021-04-06 | 中国石油化工股份有限公司 | Method for producing isomerized gasoline and aromatic hydrocarbon from alkane |
| CN115505420B (en) * | 2021-06-23 | 2024-07-16 | 中国石化工程建设有限公司 | Light naphtha orthographic structuring method |
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