CN107573964A - A kind of n-alkane low temperature isomerization method and device - Google Patents
A kind of n-alkane low temperature isomerization method and device Download PDFInfo
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Abstract
The present invention relates to a kind of n-alkane low temperature isomerization method, this method is using low-carbon n-alkane and hydrogen as raw material, using the low temperature isomerization catalyst of chlorinated aluminas loading platinum, reacted in isomerization reactor, products therefrom is after stabilizer carries out gas-liquid separation, by the direct Returning reactor of more than 50% gas-phase product, remaining gas-phase product discharges battery limit (BL) after physical absorption dechlorination, and liquid product is collected as isomerization product.Invention also provides a kind of n-alkane low temperature isomerization unit, including connected reactor and stabilizer；The gaseous stream pipeline on the stabilizer top is connected with the reactor and dechlorination tank respectively；The liquid phase stream pipeline of the stable tower bottom is connected with isomerized oil product zone.The present invention has the characteristics of significantly reducing hydrogen usage and chlorinating agent dosage, can greatly improve as the environmental problem caused by hydrogen chloride, and significantly reduce running cost and cost of investment.
Description
Technical field
The present invention relates to a kind of oil-refining chemical field, and in particular to a kind of n-alkane low temperature isomerization method and device.
Background technology
In recent years, the isomery chemical industry using the difunctional low temperature isomerization catalyst of chlorinated aluminas loading platinum as representative
Skill, due to compared with high liquid yield, cracking reaction is few, high isomerization is active and high stability, obtained more and more extensive
Application.
Typical low temperature isomerization process is mainly made up of drying unit, reaction member, stable unit and caustic wash unit.Work
Skill flow chart is shown in accompanying drawing 1.Specifically, dried n-alkane raw material and dried hydrogen are mixed, by heater
Entering reactor after heating, reaction system is the reactor of two serial operations, and the operation temperature of first reactor is higher,
Reacted with higher reaction speed, the operation temperature of second reactor is lower, is advantageous to thermodynamical equilibrium raising
Catalyst activity.Product enters product stabilizer after heat exchange after reaction, and overhead stream is released after caustic wash tower washs and removes HCl
Deflation is discharged into fuel gas system, and stabilizer tower base stream then goes out device and goes to isomerization product area.Injected in fill process few
Organic chloride is measured, with the HCl of supplement loss.
Common isomerization process such as UOP HOT Penex isomerization process, the BP/PSA isomerization process of BP companies and
The ABBLUMMUS isomerization process of LUMMUS companies and IFP Hexorb isomerization process, using above-mentioned technique, catalyst
It is the bifunctional catalyst of chlorinated aluminas loading platinum, reaction temperature is 120~180 DEG C, the low temperature isomerization catalytic
Agent has higher reactivity, higher liquid yield, high isomerization selectivity and stability, but because catalyst is to water
Point, the impurity such as oxide and sulphur it is very sensitive, the loss of chlorine easily occurs during the course of the reaction, it is therefore desirable to be continuously added into organic
Chloride carries out benefit chlorine, and can produce HCl because chlorinating agent decomposes, and easily equipment is caused to corrode, and product is polluted,
So needing to set the HCl in scrubbing tower and in isomerization product, the alkali cleaning column overhead stream after neutralization is discharged into as release gas
Fuel gas system.The selection of this kind of technique, caused spent lye is caused easily to pollute environment first；Secondly the H in release gas2With
HCl etc. can not be utilized effectively, cause the wasting of resources；Furthermore add investment cost and operating cost.
UOP HOT Penex isomerization process be light naphthar raw material first pass through the drier equipped with molecular sieve slough it is micro-
Measure moisture content, certain purity hydrogen (equivalent to reform hydrogen purity) by being compressed after gas-drying apparatus through hydrogen compressor, then with original
Material mixing, through with entering reactor after reaction discharging heat exchange and steam heating, reaction system is the reaction of two serial operations
Device, the operation temperature of first reactor is slightly higher, and to reach the high reaction speed of comparison, the operation temperature of second reactor is slightly
It is low, advantageously to improve catalyst activity in thermodynamical equilibrium.It is steady that reaction product enters product after being exchanged heat with fresh feed
Determine tower, overhead gas circulate through tail gas alkaline cleaning tower and fuel gas system is discharged into after washing removes micro hydrogen chloride, bottom of towe isomerization production
Product can be used as gasoline concoction component after going out device.
BP isomerization process is developed by British Petroleum Company (BP), is externally announced first within 1962, nineteen sixty-five first set work
Industry device is gone into operation.BP flows are similar to Penex.C5/C6 raw materials after desulfurization mix with recycle hydrogen, anti-by first after heated
Answer device to make aromatic hydrocarbons and alkene saturation, and normal hydrocarbon is converted into isohydrocarbon, enter second reactor after reaction product cooling, low
Further isomerization under the conditions of temperature, high-pressure separator, the gas isolated and a small amount of supplement hydrogen are entered after reaction product cooling
Reactor is circulated back to, liquid then enters stabilizer, and stable overhead gas enter in fuel gas after alkali cleaning removes de-chlorine hydride, tower
Bottom isomerized oil is gasoline concoction component.A small amount of organic chloride is injected in charging, with the hydrogen chloride of supplement loss.
Isomerization process flow, raw material remove the C4 and C5/C6 of LUMMUS companies with supplement hydrogen through molecular sieve drying tanks altogether
Water and other trace contaminants, right latter two material mixing, reach reaction temperature through heat exchanger and heater, anti-into fixed bed
Answer device.AT-2 and AT-2G catalyst for carry chlorine platinum/aluminum oxide, 115~182 DEG C, 2.4~3.1MPa of pressure of reaction temperature,
Keep compared with can reach higher catalyst stability under conditions of low hydrogen/gasoline ratio, so as to not use the flow that hydrogen circulates,
A small amount of organic chloride is injected in actual mechanical process, in charging to keep the acidity of catalyst.C4 and C5/C6 isomerization
Product enters product stabilizer, enters fuel system after alkali cleaning containing lighter hydrocarbons and a small amount of hydrogen, the tower top fraction of hydrogen chloride.
Hexorb techniques are the energy-saving isomerization process that french petroleum research institute (IFP) releases, using molecular sieve
Positive isohydrocarbon is separated into isomerization processes by pressure swing adsorption.Raw material enters reaction after de- isopentane tower separates isopentane
Device, isomerization reaction is carried out under cryogenic, sieve pressure-variable adsorption through gas molecule in space, realize being kept completely separate for positive isohydrocarbon.
A small amount of organic chloride is injected in charging, with the hydrogen chloride of supplement loss, the overhead gas of containing hydrogen chloride enter after alkali cleaning
Fuel system.
CN104169243A discloses the method and apparatus for isomerization of paraffinic hydrocarbons, using two separators by stabilizer
HCl and H is rich in overhead vapor stream2Stream separated with C5- hydrocarbon flows, will be enriched in HCl and H2Stream introduce in isomerization bar
In the reactor operated under part with by isomerization catalyst contained therein activate and formed chloride promotion isomerization catalyst.
Make the isomerization catalyst that paraffinic feed stream and chloride promote in the reactor, contact in the presence of hydrogen gas with by alkane
Hydrocarbon isomerization.Depleted HCl is sent into caustic wash tower processing rich in C5- hydrocarbon flows.Although to a certain extent may be used using this method
To reduce the dosage of chlorinating agent and hydrogen, but due to the setting of high score separator and caustic wash tower, considerably increase cost of investment
And running cost, and the setting of caustic wash tower unavoidably brings a series of environmental problems, is unfavorable for environmental protection.
US4804803 discloses one way hydrogen isomerization method and prepares isomerized oil, using anti-including drying unit, isomerization
The technique for answering unit, stable unit and caustic wash unit.The technique uses the bifunctional catalyst of chlorinated aluminas loading platinum,
Course of reaction persistently mends chlorine and hydrogen make-up, keeps isomerization catalyst activity, by caustic wash unit and HCl, after neutralization
Discharge gas incoming fuel area.Still there is environmental problem caused by HCl in the technique, and increase cost of investment and running cost.
In summary, environmental problem caused by HCl caused by solving injection chlorinating agent decomposition, reduces disappearing for chlorinating agent
Consumption, it is the difunctional isomerization catalyst catalysis n-alkane low temperature isomery for improving currently employed chlorinated aluminas loading platinum
The key of chemical industry skill.
The content of the invention
The defects of it is an object of the invention to overcome prior art, there is provided a kind of n-alkane low temperature isomerization method, should
Method by hydrogen and hydrogen chloride Returning reactor by promoting n-alkane low temperature isomerization reaction, so as to which chlorinating agent be greatly decreased
With hydrogen injection amount, and running cost and cost of investment are significantly reduced.
Specifically, the invention provides a kind of n-alkane low temperature isomerization method, this method is with low-carbon n-alkane
It is raw material with hydrogen, using the low temperature isomerization catalyst of chlorinated aluminas loading platinum, is carried out in isomerization reactor
Reaction, after products therefrom carries out gas-liquid separation in stabilizer, by the direct Returning reactor of more than 50% gas-phase product, remaining
Gas-phase product discharges battery limit (BL) after physical absorption dechlorination, and liquid product is collected as isomerization product.
Low-carbon n-alkane of the present invention refers to the one or more in C4~C7 hydro carbons, preferably in C4~C6 hydro carbons
One or more.In actual production, the raw material specifically includes liquefied petroleum gas, reforming topped oil, Aromatic raffinate, hydrogenation
Device light naphthar etc..
Preferably described reaction of the invention is to face hydrogen low temperature isomerization reaction.Wherein reaction pressure is 2.0~4.0MPa, temperature
For 100~180 DEG C.
Gas-phase product of the present invention mainly includes H2, HCl and C5- lighter hydrocarbons.It is of the invention to be found by many experiments, pin
To the isomerization catalyst of chlorinated aluminas loading platinum, above-mentioned gas-phase product is (especially through above-mentioned specified temp and pressure
Gas-phase product obtained by conditioned response) need not move through lighter hydrocarbons separation and direct Returning reactor, will not only hinder reaction carry out,
H can be promoted on the contrary2Contacted with HCl with n-alkane raw material and more effectively activate isomerization catalyst, so as to promote isomery
Change the progress of reaction.Aforesaid operations are not only greatly reduced chlorinating agent and supplement the consumption of hydrogen, enter also without to gas-phase product
The further working process of row, avoids the wasting of resources, increases economic efficiency.
The gas-phase product ratio of Returning reactor of the present invention is more than 50%, as the increase of ratio is to H2And HCl
Utilization rate increase, but recycle compressor need to be used during due to Returning reactor, if returning to ratio increase circulation can be caused to compress
Function consumption increase, so as to increase running cost.Therefore, the ratio can be according to practical condition and needs 50%~100%
Between be adjusted, preferably 80~99%.Accordingly, in actual production, the recycle ratio of the recycle compressor of use is preferred
For more than 50%, more preferably 80~99%, although can be improved to H with the increase of recycle ratio2With HCl utilization rate, but together
When can also increase energy consumption and running cost, therefore, it is suitable to be needed to select according to production cost and production in actual production
The compressor of recycle ratio.
The present invention adsorbs the hydrogen chloride in gas-phase product by the way of physical absorption dechlorination, saves the setting of caustic wash tower,
Spent lye process problem caused by washing neutralization is avoided simultaneously, it is green and easy to operation, reduce investment outlay and grasp
Make expense.The adsorbent that the physical absorption dechlorination uses is not done from the conventional dechlorination adsorbent in this area, the present invention
Particular determination.In actual production, the physical absorption dechlorination process can be carried out in dechlorination tank.
Because the present invention is without directly reusing or reclaiming to gas-phase product progress lighter hydrocarbons separation, in order to ensure this is mixed
The hydrogen chloride closed in gas-phase product is fully absorbed, and the present invention carries out preferred to the operating pressure and temperature of dechlorination.Specifically,
During preferred dechlorination of the invention temperature be 30~80 DEG C, pressure be 1.0~3.0MPa, more preferably temperature is 40~60 DEG C, and pressure is
1.5~2.5MPa.
Present invention simultaneously provides a kind of device of n-alkane low temperature isomerization, the device greatly improves to be drawn by hydrogen chloride
The environmental problem risen, makes easy to operation.
Specifically, described device includes connected reactor and stabilizer；The gas gas-phase objects flow tube on the stabilizer top
Road is connected with the reactor and dechlorination tank respectively；The liquid phase stream pipeline and isomerized oil product zone phase of the stable tower bottom
Even.
Wherein, in order to ensure the smooth Returning reactor of gaseous stream on the stabilizer top, in the gas of Returning reactor
Recycle gas compressor, while the gaseous stream and raw hydrogen common recycle air compressor are set on phase logistics pipeline.
In order to improve reaction conversion ratio, the reactor may be configured as two groups of reactors of series connection, i.e., first reactor and
Second reactor.Now, the gaseous stream pipeline on the stabilizer top is through recycle gas compressor and first first reactor
It is connected.
In said apparatus, isomerization reaction product is separated into top gaseous phase logistics and tower by being provided for of the stabilizer
Bottom liquid phase stream, top gaseous phase logistics include H2, HCl and C5- lighter hydrocarbons, bottom of towe liquid phase stream is isoparaffin product.It is described to follow
Ring air compressor is provided for stablize under cycling condition that top gaseous phase logistics is at least most of is recycled back into foregoing isomery
Change reactor.The stable tower top that at least most of return comes that is provided for receiving of the reactor is rich in H2, HCl and C5- it is light
The gaseous stream of hydrocarbon, carry out the isomerization reaction of positive structure low-carbon alkanes.Being provided for for the dechlorination tank is thorough under the conditions of dechlorination
Bottom absorbs a small amount of stabilizer top gaseous phase logistics.
N-alkane low temperature isomerization method provided by the invention and equipment, by the way that hydrogen and hydrogen chloride are returned into reaction
Device, the method that a small amount of hydrogen chloride carries out dechlorination absorption, effectively carries out the low temperature isomerization reaction of positive structure low-carbon alkanes.It will can stablize
Top gaseous phase logistics is recycled back into reaction system, will be enriched in H2, HCl and C5- lighter hydrocarbons logistics contacted with n-alkane raw material,
Effective activation isomerization catalyst, promote the progress of isomerization reaction, chlorinating agent is greatly reduced and supplements the consumption of hydrogen, keeps away
Exempt from the wasting of resources, increase economic efficiency.HCl is recycled, saves the setting of caustic wash tower, while avoids washing and neutralizes institute's band
The spent lye process problem come, hence it is evident that improve environmental pollution, and save equipment investment.Dechlorination tank is set to inhale a small amount of HCl
Dechlorination is received, it is easy to operation, reduce investment outlay and operating cost.
Brief description of the drawings
Fig. 1 is the process flow diagram of typical n-alkane low temperature isomerization；
Fig. 2 is n-alkane low temperature isomerization unit of the present invention and method flow schematic diagram；Wherein：1st, mixture
Stream, 2, first reactor, 3, one anti-product, 4, second reactor, 5, two anti-products, 6, stabilizer, 7, stable top gaseous phase thing
Flow (pipeline), 8, stabilizer bottom liquid phase stream (pipeline), 9, rich in HCl and H2Top gaseous phase logistics (pipeline), 10, circulating air
Compressor, 11, pipeloop, 12, depleted HCl and H2Top gaseous phase logistics (pipeline), 13, dechlorination tank, 14, release gas (pipe
Road), 15, release gas battery limit (BL), 16, isomerized oil product zone.
Embodiment
Below in conjunction with the accompanying drawing in the embodiment of the present invention, the technical scheme in the embodiment of the present invention is carried out clear, complete
Whole description.Based on embodiments of the invention, those of ordinary skill in the art are obtained under the premise of creative work is not made
The every other embodiment obtained, belongs to the scope of protection of the invention.Embodiment is as follows：
Embodiment 1
A kind of n-alkane low temperature isomerization unit is present embodiments provided, partly with reference to shown in figure 2, described device includes
First reactor 1, second reactor 4 and the stabilizer 6 being sequentially connected；The gaseous stream pipeline 7 on the stabilizer top is distinguished
It is connected with the first reactor 1 and dechlorination tank 13；The liquid phase stream pipeline 8 of the stable tower bottom and isomerized oil product zone
16 are connected；Wherein, recycle gas compressor 10 is set on the pipeloop 11 of Returning reactor.
Embodiment 2
The present embodiment uses the device n-alkane low temperature isomerization that embodiment 1 provides.Detailed process is：
Mixed logistics 1 is carried out by the dried low-carbon n-alkane raw material of drier and dried supplement hydrogen,
Exchanged heat by feed exchanger, feed heater heating, the first time isomerization reaction into isomerization reactor 2, for the first time
Product 3 goes successively to second of the isomerization reaction of generation of isomerization reactor 4 after reaction.Product 5 enters into stabilizer 6 after reaction
Row gas-liquid separation, isomerization reaction product is separated into top gaseous phase logistics 7 and bottom of towe liquid phase stream 8, top gaseous phase logistics 7 is wrapped
Containing H2, HCl and low-carbon lighter hydrocarbons, bottom of towe liquid phase stream 8 be isoparaffin product.At least most of logistics of top gaseous phase logistics (accounts for
Gaseous stream total amount 50% and be rich in HCl and H2) 9 process recycle compressors 10, isomerization is recirculated back to by pipeline 11
Reactor 1 carries out above-mentioned isomerization reaction；Stable tower base stream 8 then enters product zone 16 as isomerization product；Stable tower top
A small amount of gaseous stream (depleted HCl) 12, which enters dechlorination tank 13, to carry out thoroughly absorbing dechlorination, dechlorination tank operating condition：Operation pressure
Power is 1.5MPa, 40 DEG C of operation temperature.Release gas 14 after dechlorination goes to battery limit (BL) 15.
Under these conditions, the injection rate of chlorinating agent and hydrogen can reduce 50% respectively, the dechlorinated tank of a small amount of tail gas of tower top
Battery limit (BL) is discharged into after absorption.
Embodiment 3
The present embodiment uses the device n-alkane low temperature isomerization that embodiment 1 provides.Detailed process is：
Mixed logistics 1 is carried out by the dried low-carbon n-alkane raw material of drier and dried supplement hydrogen,
Exchanged heat by feed exchanger, feed heater heating, the first time isomerization reaction into isomerization reactor 2, for the first time
Product 3 goes successively to second of the isomerization reaction of generation of isomerization reactor 4 after reaction.Product 5 enters into stabilizer 6 after reaction
Row gas-liquid separation, isomerization reaction product is separated into top gaseous phase logistics 7 and bottom of towe liquid phase stream 8, top gaseous phase logistics 7 is wrapped
Containing H2, HCl and low-carbon lighter hydrocarbons, bottom of towe liquid phase stream 8 be isoparaffin product.At least most of logistics of top gaseous phase logistics (accounts for
Gaseous stream total amount 70% and be rich in HCl and H2) 9 process recycle compressors 10, isomerization is recirculated back to by pipeline 11
Reactor 1 carries out above-mentioned isomerization reaction；Stable tower base stream 8 then enters product zone 16 as isomerization product；Stable tower top
A small amount of gaseous stream (depleted HCl) 12, which enters dechlorination tank 13, to carry out thoroughly absorbing dechlorination, dechlorination tank operating condition：Operation pressure
Power is 2MPa, 50 DEG C of operation temperature.Release gas 14 after dechlorination goes to battery limit (BL) 15.
Under these conditions, the injection rate of chlorinating agent and hydrogen can reduce 70% respectively, the dechlorinated tank of a small amount of tail gas of tower top
Battery limit (BL) is discharged into after absorption.
Embodiment 4
The present embodiment uses the device n-alkane low temperature isomerization that embodiment 1 provides.Detailed process is：
Mixed logistics 1 is carried out by the dried low-carbon n-alkane raw material of drier and dried supplement hydrogen,
Exchanged heat by feed exchanger, feed heater heating, the first time isomerization reaction into isomerization reactor 2, for the first time
Product 3 goes successively to second of the isomerization reaction of generation of isomerization reactor 4 after reaction.Product 5 enters into stabilizer 6 after reaction
Row gas-liquid separation, isomerization reaction product is separated into top gaseous phase logistics 7 and bottom of towe liquid phase stream 8, top gaseous phase logistics 7 is wrapped
Containing H2, HCl and low-carbon lighter hydrocarbons, bottom of towe liquid phase stream 8 be isoparaffin product.At least most of logistics of top gaseous phase logistics (accounts for
Gaseous stream total amount 90% and be rich in HCl and H2) 9 process recycle compressors 10, isomerization is recirculated back to by pipeline 11
Reactor 1 carries out above-mentioned isomerization reaction；Stable tower base stream 8 then enters product zone 16 as isomerization product；Stable tower top
A small amount of gaseous stream (depleted HCl) 12, which enters dechlorination tank 13, to carry out thoroughly absorbing dechlorination, dechlorination tank operating condition：Operation pressure
Power is 2.5MPa, 55 DEG C of operation temperature.Release gas 14 after dechlorination goes to battery limit (BL) 15.
Under these conditions, the injection rate of chlorinating agent and hydrogen can reduce 90% respectively, the dechlorinated tank of a small amount of tail gas of tower top
Battery limit (BL) is discharged into after absorption.
Embodiment 5
The present embodiment uses the device n-alkane low temperature isomerization that embodiment 1 provides.Detailed process is：
Mixed logistics 1 is carried out by the dried low-carbon n-alkane raw material of drier and dried supplement hydrogen,
Exchanged heat by feed exchanger, feed heater heating, the first time isomerization reaction into isomerization reactor 2, for the first time
Product 3 goes successively to second of the isomerization reaction of generation of isomerization reactor 4 after reaction.Product 5 enters into stabilizer 6 after reaction
Row gas-liquid separation, isomerization reaction product is separated into top gaseous phase logistics 7 and bottom of towe liquid phase stream 8, top gaseous phase logistics 7 is wrapped
Containing H2, HCl and low-carbon lighter hydrocarbons, bottom of towe liquid phase stream 8 be isoparaffin product.At least most of logistics of top gaseous phase logistics (accounts for
Gaseous stream total amount 95% and be rich in HCl and H2) 9 process recycle compressors 10, isomerization is recirculated back to by pipeline 11
Reactor 1 carries out above-mentioned isomerization reaction；Stable tower base stream 8 then enters product zone 16 as isomerization product；Stable tower top
A small amount of gaseous stream (depleted HCl) 12, which enters dechlorination tank 13, to carry out thoroughly absorbing dechlorination, dechlorination tank operating condition：Operation pressure
Power is 3MPa, 60 DEG C of operation temperature.Release gas 14 after dechlorination goes to battery limit (BL) 15.
Under these conditions, the injection rate of chlorinating agent and hydrogen can reduce 95% respectively, the dechlorinated tank of a small amount of tail gas of tower top
Battery limit (BL) is discharged into after absorption.
Embodiment 6
The present embodiment uses the device n-alkane low temperature isomerization that embodiment 1 provides.Detailed process is：
Mixed logistics 1 is carried out by the dried low-carbon n-alkane raw material of drier and dried supplement hydrogen,
Exchanged heat by feed exchanger, feed heater heating, the first time isomerization reaction into isomerization reactor 2, for the first time
Product 3 goes successively to second of the isomerization reaction of generation of isomerization reactor 4 after reaction.Product 5 enters into stabilizer 6 after reaction
Row gas-liquid separation, isomerization reaction product is separated into top gaseous phase logistics 7 and bottom of towe liquid phase stream 8, top gaseous phase logistics 7 is wrapped
Containing H2, HCl and low-carbon lighter hydrocarbons, bottom of towe liquid phase stream 8 be isoparaffin product.At least most of logistics of top gaseous phase logistics (accounts for
Gaseous stream total amount 99% and be rich in HCl and H2) 9 process recycle compressors 10, isomerization is recirculated back to by pipeline 11
Reactor 1 carries out above-mentioned isomerization reaction；Stable tower base stream 8 then enters product zone 16 as isomerization product；Stable tower top
A small amount of gaseous stream (depleted HCl) 12, which enters dechlorination tank 13, to carry out thoroughly absorbing dechlorination, dechlorination tank operating condition：Operation pressure
Power is 1.5MPa, 40 DEG C of operation temperature.Release gas 14 after dechlorination goes to battery limit (BL) 15.
Under these conditions, the injection rate of chlorinating agent and hydrogen can reduce 99% respectively, the dechlorinated tank of a small amount of tail gas of tower top
Battery limit (BL) is discharged into after absorption.
Comparative example 1
Mixed by the dried low-carbon n-alkane raw material of drier and dried supplement hydrogen, changed by charging
The heat exchange of hot device, feed heater heating, the first time isomerization reaction into isomerization reactor, after first set reaction product after
Second of isomerization reaction occurs for the continuous isomerization reactor that enters.Product enters stabilizer progress gas-liquid separation after reaction, will be different
Structure reaction product is separated into top gaseous phase logistics and bottom of towe liquid phase stream, and top gaseous phase logistics includes H2, HCl and low-carbon it is light
Hydrocarbon, bottom of towe liquid phase stream are isoparaffin product.Top gaseous phase logistics carries out washing neutralization into caustic wash tower, the release after neutralization
Gas goes out battery limit (BL) as fuel gas, and stable tower base stream then enters product zone as isomerization product.
Under these conditions, the injection rate of chlorinating agent and hydrogen does not have any change, is injected according to normal injection rate.Evaluation
As a result it is as shown in table 1 below.
Table 1
It is can be seen that by the data of table 1 after implementing that top gaseous phase logistics return isomerization reactor unit will be stablized, with
The gas ratio increase of Returning reactor, hydrogen injection amount and chlorinating agent injection rate gradually decrease, compared with comparative example 1, when
The gas ratio of Returning reactor be 99% when, hydrogen and chlorinating agent injection can reduce 99% injection rate, can obviously reduce and contain
Chlorine discharges the discharge of gas, greatly improves environmental problem, shows that the method for the present invention has reached expected purpose.
Although above the present invention is made to retouch in detail with general explanation, embodiment and experiment
State, but on the basis of the present invention, it can be made some modifications or improvements, this is apparent to those skilled in the art
's.Therefore, these modifications or improvements without departing from theon the basis of the spirit of the present invention, are belonged to claimed
Scope.
Claims (10)
1. a kind of n-alkane low temperature isomerization method, it is characterised in that using low-carbon n-alkane and hydrogen as raw material, using chlorine
Change the low temperature isomerization catalyst of alumina load platinum, reacted in isomerization reactor, products therefrom is stable
After tower carries out gas-liquid separation, by the direct Returning reactor of more than 50% gas-phase product, remaining gas-phase product takes off through physical absorption
Battery limit (BL) is discharged after chlorine, liquid product is collected as isomerization product.
2. according to the method for claim 1, it is characterised in that the low-carbon n-alkane refers to one in C4~C7 hydro carbons
Kind or several, the one or more preferably in C4~C6 hydro carbons.
3. according to the method for claim 1, it is characterised in that by the direct Returning reactor of 80~99% gas-phase product.
4. the method according to claim 1 or 3, it is characterised in that returned to gas-phase product instead using recycle gas compressor
Answer device.
5. according to the method for claim 1, it is characterised in that the reaction is faces hydrogen low temperature isomerization reaction, wherein instead
It is 100~180 DEG C to answer pressure, and temperature is 2.0~4.0MPa.
6. according to the method described in Claims 1 to 5 any one, it is characterised in that the temperature during physical absorption dechlorination
For 30~80 DEG C, pressure is 1~3MPa.
7. a kind of n-alkane low temperature isomerization unit, it is characterised in that including connected reactor and stabilizer；The stabilization
The gaseous stream pipeline at tower top end is connected with the reactor and dechlorination tank respectively；The liquid phase stream pipeline of the stable tower bottom
It is connected with isomerized oil product zone.
8. device according to claim 7, it is characterised in that circulation is set on the gaseous stream pipeline of Returning reactor
Air compressor.
9. device according to claim 7, it is characterised in that the reactor is anti-by the first reactor connected and second
Device is answered to form.
10. device according to claim 9, it is characterised in that the gaseous stream pipeline on the stabilizer top is through circulation
Air compressor is connected with first reactor.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109486514A (en) * | 2018-11-09 | 2019-03-19 | 北京赛诺时飞石化科技有限公司 | A kind of the low temperature isomerization method and device of the n-alkane feedstock oil containing benzene |
| CN110643389A (en) * | 2019-10-31 | 2020-01-03 | 宁夏金裕海化工有限公司 | Method and device for reducing naphtha sulfur content and improving naphtha octane number |
| CN110872527A (en) * | 2018-08-29 | 2020-03-10 | 中国石油化工股份有限公司 | C4~C6Light paraffin isomerization method |
| CN112166096A (en) * | 2018-05-03 | 2021-01-01 | 环球油品有限责任公司 | Process for isomerizing hydrocarbons |
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| CN110872527A (en) * | 2018-08-29 | 2020-03-10 | 中国石油化工股份有限公司 | C4~C6Light paraffin isomerization method |
| CN110872527B (en) * | 2018-08-29 | 2022-03-11 | 中国石油化工股份有限公司 | C4～C6Light paraffin isomerization method |
| CN109486514A (en) * | 2018-11-09 | 2019-03-19 | 北京赛诺时飞石化科技有限公司 | A kind of the low temperature isomerization method and device of the n-alkane feedstock oil containing benzene |
| CN110643389A (en) * | 2019-10-31 | 2020-01-03 | 宁夏金裕海化工有限公司 | Method and device for reducing naphtha sulfur content and improving naphtha octane number |
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