CN102226102A - Method for producing gasoline blended component with high octane number from refinery gas and light hydrocarbons - Google Patents
Method for producing gasoline blended component with high octane number from refinery gas and light hydrocarbons Download PDFInfo
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- CN102226102A CN102226102A CN2011101191712A CN201110119171A CN102226102A CN 102226102 A CN102226102 A CN 102226102A CN 2011101191712 A CN2011101191712 A CN 2011101191712A CN 201110119171 A CN201110119171 A CN 201110119171A CN 102226102 A CN102226102 A CN 102226102A
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Abstract
The invention relates to a method and device for producing a gasoline blended component with high octane number from refinery gas and light hydrocarbons, belonging to the technical field of aromatization of light hydrocarbons. The device comprises heating furnaces, reactors and an absorption-desorption tower which are serially connected, and is characterized in that: (1) two groups of the heating furnaces and the reactors that are parallelly connected are used for cycle operation; (2) in the reactor, the process conditions are as follows: the reaction temperature is 320-420 DEG C, the pressure is 0.8-2.0 MPa, the mass space velocity of 0.4-0.8 h<-1>, and the mass ratio of light hydrocarbon component to low-octane number gasoline is (30:70)-(10:90); (3) the light hydrocarbon component in the reactor is one of catalysis dry gas, coking dry gas and catalytic coking liquefied gas or a mixture thereof; and the low-octane number gasoline is one of ordinary/reduced pressure straight-run gasoline, field condensate oil, hydrogenated naphtha and cracked gasoline or any combination thereof; and (4) a stabilizer column and a heavy component eliminating tower are serially connected on the rear side of the absorption-desorption tower. The method and the device provided by the invention adopt two groups of the heating furnaces and the reactors that are parallelly connected for cycle operation, so as to realize continuous operation of reaction regeneration. In addition, the method and the device have strong adaptability and low energy consumption, and can directly remove part of the heavy components in the gasoline component so as to reduce the dry point of the gasoline product. During regeneration, the suction pressure regeneration combined process is used, so as to greatly shorten the coking time.
Description
Technical field
The invention belongs to light-hydrocarbon aromatized technical field, specifically be a kind of refinery gas with reformation tops, condensate oil, hydrogenation after the mixing raw material of compositions such as coking naphtha and virgin naphtha on fixed-bed reactor, contact and carry out the method that the stop bracket gasoline blend component is produced in the upgrading reaction with modifying catalyst.
Background technology
Along with China carries out the appearance of white gasoline and new gasoline standard comprehensively, country is more and more stricter to the specification of quality of gasoline product, requires more and more lower to sulfur in gasoline content, metal content, olefin(e) centent.The sulphur content in traditional reduction gasoline and the method for olefin(e) centent are exactly nothing but gasoline selective hydrogenation and reformer etc., but ubiquity production cost height, complex process is unfavorable for large-area popularization.That adopts at present usually passes through to add the method that the metal octane promoter improves gasoline octane rating, and add-on will be subjected to strict control in the long run, or will be banned.Simultaneously, the part low octane value gasoline is for example reformed in the refinery, and petroleum naphtha such as coking naphtha and straight-run spirit does not have good outlet behind tops, condensate oil, the hydrogenation.Therefore, the technology that can produce the higher clean gasoline blend component of low alkene, low-sulfur and octane value receives much concern.
On the other hand, the refinery gas that refinery's by-product is a large amount of mainly contains dry gas and liquefied gas two portions.Oil refinery dry gas is big with catalytic cracked dry gas output especially, but the volume fraction height of contained ethene and lighter hydrocarbons in the catalytic cracked dry gas has utility value.But at present oil refinery dry gas is all sent into the gas pipe network usually and is made fuel gas usefulness, some in addition put into torch and burn, not only can cause environmental pollution, still one of resource waste greatly.Simultaneously, C4 olefin(e) centent higher (about 70%) in refinery's liquefied gas.Therefore, how optimizing the alkene resource of utilizing in the refinery is one of difficult problem of facing of China's petrochemical industry.
Publication number is that the Chinese patent of 1032697C discloses a kind of inferior gasoline upgrading-aromatization method, this method can be converted into straight-run spirit the gasoline blend component of high aromaticity content, adopt the multi-stage type reaction process, raw material enters first reactor, at 300～500 ℃, 0.05～1.2MPa, weight space velocity is to react under 0.2～1.0 the conditions of non-hydrogen, resultant is through vapor-liquid separation, the above liquid of C5 by fractionation after, obtain gasoline fraction, after in second reactor, carrying out aromatization less than the gas of C4 in the reactant, condition is 480～650 ℃, 0.05～1.5MPa, volume space velocity is 20～2000, the aromizing product obtains being rich in the gas and the aromatic hydrocarbons mixture of hydrogen after gas-liquid separation.This method has effectively utilized the low molecular hydrocarbon that produces in the inferior gasoline upgrading process, liquid is received and the gasoline octane rating raising, but contained more last running in the aromizing product, does height, needs cutting, and the dry gas yied in the reaction is up to more than 7%.The catalyzer one way life-span was about for two weeks, needed a plurality of reactors to switch regeneration in turn, and plant investment is higher.
Publication number is 1485414 Chinese patent, disclose the technology of a kind of catalytically cracked gasoline non-hydrogen aromatization and desulfurization: the lighting end after full cut of catalytically cracked gasoline or the process fractionation enters an aromizing desulphurization reactor, carry out the alkene aromatization, the hydrodesulfurization reaction that the hydrogen that utilizes aromatization to produce carries out full cut or last running, reduce olefin content in gasoline and sulphur content, then with the reaction product alkali-free sweetening, the gasoline products that obtains, its octane value can remain basically stable with upgrading before.
The Chinese patent that is disclosed as 1600836A discloses the method that the straight-run spirit upgrading prepares gasoline with low olefine content, this method with straight-run spirit with after the C 4 olefin cut mixes, under 0.2～0.6MPa, 300～500 ℃ of conditions with catalyzer contact reacts, the dry gas in the separated product, liquefied gas and gasoline component then.This method can effectively utilize carbon four components in the refinery that straight-run spirit is carried out upgrading, produces high-octane rating and the low gasoline component of olefin(e) centent.But contain more last running in the reaction product, doing height needs cutting; Reaction pressure is low, and reaction depth is not enough, amount of finish is little; Reactor is provided with unreasonable, and reactor batch temperature should not be controlled; Absorbing-stabilizing system adopts compressor pressurizes, bottom reboiler thermal source to adopt steam, and system flow is unreasonable, and plant investment is big, tooling cost is high; The straight-run spirit raw material sources are limited, are not easy to satisfy the needs that alkene falls in oil refinery gasoline.
Publication number is the catalysis conversion method that 1814713 Chinese patent discloses a kind of liquefied gas and gasoline feeding at same time, stock oil/liquefied gas enters with catalyzer from riser tube or fluidized-bed bottom and contacts, and reacted oil gas enters water ice condenser and carries out vapor-liquid separation.Reaction process can make content of olefin in gasoline descend, and aromaticity content increases; Can guarantee that under certain condition the liquid fraction in reaction product liquid yield and the charging maintains an equal level or increase.
Summary of the invention
The present invention is a kind of to utilize mixing raw material that low octane value gasoline and refinery gas form to contact the method for carrying out upgrading on multi-stage fixed-bed with catalyzer, can be under comparatively gentle reaction conditions, low-octane gasoline is converted into low, the low-sulfur content clean gasoline blend component of olefin(e) centent, liquefied gas is converted into the high-quality liquefied gas that olefin(e) centent is less, can be used as the motor liquified gas use, alkene in the dry gas is fully recycled, has good economic benefits and social benefit.
The concrete technical scheme that the present invention adopts is:
A kind of refinery gas, lighter hydrocarbons are produced the method for stop bracket gasoline blend component, comprise process furnace, reactor and the absorption Analytic Tower of serial connection, it is characterized in that,
1) process furnace and the reactor of two groups of parallel connections of employing, cyclical operation; When the catalyst carbon deposition in the reaction period seriously need be regenerated, will need regenerated process furnace and reactor assembly to cut out, another group is still carried out ordinary production, the production of the device integral body amount of falling.The operation of realization response regenerated continuity.
2) in the reactor, processing condition are: 320～420 ℃ of temperature of reaction, and pressure 0.8～2.0MPa, mass space velocity are 0.4～0.8h-1, the mass ratio of light hydrocarbon component and low octane value gasoline is 30: 70～10: 90;
3) the interior light hydrocarbon component of reactor is a kind of or its mixture in catalysis drying gas, coking dry gas or the catalytic coking liquefied gas; Described low octane value gasoline is a kind of or its arbitrary combination in straight-run spirit, field condensate, hydrotreated naphtha, the pyrolysis gasoline of often reducing pressure;
4) serial connection stabilizer tower and weight-removing column behind the described absorption Analytic Tower.
For convenience of the temperature of reaction in the controlling reactor, preferred version of the present invention is: a hydrogen hydrocarbon component part is with after low octane value gasoline mixes, enter reactor after process furnace is heated to 320～420 ℃, remainder enters second and third bed of reactor after adding the heat vapourizer vaporization.
A kind of refinery gas, lighter hydrocarbons are produced the device of stop bracket gasoline blend component, it is characterized in that,
Comprise first process furnace, first reactor, the first reactor bottom discharge nozzle is successively through the first reaction product interchanger, the first reaction product aftercooler, and serial connection absorbs Analytic Tower, stabilizer tower and weight-removing column successively then;
Comprise that also second process furnace and second reactor and first process furnace, first reactor are in parallel, the second reactor bottom discharge nozzle is successively through the second reaction product interchanger, the second reaction product aftercooler, and serial connection absorbs Analytic Tower, stabilizer tower and weight-removing column successively then;
The light hydrocarbon component fresh feed pump is connected first process furnace, second process furnace respectively with behind the first reaction product interchanger, the second reaction product interchanger with the gasoline feeding pump, enters first reactor and the second reactor head feed-pipe then respectively;
First, second reactor with burn jar, recycle gas compressor and the circulation of first, second reaction product interchanger be connected, also is provided with evacuation burning on jar and the recycle gas compressor connecting pipeline.
Compared with prior art, advantage of the present invention is:
1) process furnace and the reactor of two groups of parallel connections of employing, cyclical operation; When the catalyst carbon deposition in the reaction period seriously need be regenerated, will need regenerated process furnace and reactor assembly to cut out, another group is still carried out ordinary production, the production of the device integral body amount of falling.The operation of realization response regenerated continuity, the shutting down number of times of minimizing device.
2) reactor internal reaction pressure of the present invention is higher than the 0.2-0.6MPa of prior art, increases the degree of depth of reaction; Carbon four compressors of cancellation back cut down the consumption of energy, and increase the integral benefit of device.
3) method and apparatus suitability of the present invention is good, can be used in catalysis drying gas, coking dry gas and inferior patrol.
4) the present invention adopts absorption to resolve coaxial configuration and thermal source and charging process furnace combination process and greatly reduces plant energy consumption; Increase the aromatic hydrocarbons weight-removing column behind the stabilizer tower with the part heavies removal in the gasoline component, reduce doing of product gasoline; Efficient, the environment protection desulphurization refined unit of the laggard face later of product separation make gasoline products satisfy state III, state IV, state V standard.
Adopt negative pressure regenerative combination technology that the time of burning is shortened significantly when 5) regenerating.
Description of drawings
Fig. 1 is an equipment connection diagram of the present invention;
Among the figure, 1-light hydrocarbon component fresh feed pump, the 2-first reaction product interchanger, 3-first process furnace, the 4-first reaction product aftercooler, 5-first reactor, 6-absorbs Analytic Tower, 7-stabilizer tower, 8-weight-removing column, the 9-recycle gas compressor, the 10-evacuation, 11-burns jar, 12-second reactor, 13-second process furnace, the 14-second reaction product aftercooler, the 15-second reaction product interchanger, 16-gasoline feeding pump, 17-adds heat vapourizer.
Embodiment
As shown in Figure 1, light hydrocarbon component mixes through light hydrocarbon component fresh feed pump 1 a pressurization back part and the gasoline after gasoline feeding pump 16 pressurizes, and mixing raw material divides two-way to be heated to 320～420 ℃ through the first reaction product interchanger 2 (or second reaction product interchanger 15), the first reaction product interchanger 4 (or second reaction product interchanger 15), first process furnace 3 (or second process furnace 13) respectively to enter first reactor 5 (or second reactor 12) and react; Another part enters second and third section bed of first reactor 5 (or second reactor 12) then after adding heat vapourizer 17 vaporizations, answer the temperature in of bed in order to adjusting.Reaction product is come out from first reactor 5 (second reactor 12), through with the first reacting replacing heat device 2, the first reaction product aftercooler 4 (or the second reacting replacing heat device 15, the second reaction product aftercooler 14) postcooling to 40 ℃, enter and absorb desorption tower 6.The dry gas that parses is drawn from top of tower, the blending ingredients of bottom, and a part is returned to absorb in the Analytic Tower 6 after the convection zone heating of charging process furnace and is done thermal source, and another part directly enters stabilizer tower 7.Liquefied gas separates in stabilizer tower 7 with gasoline products, the liquid of top of the tower gasification through after cold but the back carrying device; Gasoline products enters and goes out device after weight-removing column 8 removes heavy constituent at the bottom of the tower.
Along with the carrying out of reaction, the coking amount on the catalyzer can progressively increase, and when quality product can not meet the demands, needs reaction is stopped, and carries out the reactor coke burning regeneration and handles.This programme design two cover heated reaction systems, the operation of the device amount of falling realizes online burning during regeneration.
Burn with first process furnace 3 and first reactor 5 and to be treated to example:
Before burning beginning, start reprocessing cycle air compressor 9 earlier, introduce nitrogen from the suction port of compressor, the nitrogen of supercharging through 3 heating of first process furnace, enters first reactor 5 and carries out hot nitrogen purge operations then through the first reaction product interchanger 2, the gas that is gone out by first reactor 5 is after the first reaction product interchanger 2,4 coolings of the first reaction product aftercooler, enter and burn jar 11, the intermittently oil extraction of jar end is progressively to take the oil gas in the reactor out of.Oil gas in first reactor 5 reaches safety requirements, and first reactor, 5 temperature ins reach when burning the temperature that needs, and from evacuation 10 introducing airs, begins to burn operation, requires Control Circulation gas initial oxygen concentration not to be higher than 0.5v%.Progressively improve oxygen level in the circulation gas according to the reactor situation of burning, when the oxygen level in the regeneration recycle gas reaches the concentration of oxygen in the air, and after not having temperature rise in first reactor 5, burn end, can replace system this moment with nitrogen purging, after oxygen level in the system is qualified, but just ordinary production is carried out in oil-feed.The catalyst regeneration burning process approximately needs ten day time.
Claims (3)
1. a refinery gas, the lighter hydrocarbons method of producing the stop bracket gasoline blend component comprises it is characterized in that process furnace, reactor and the absorption Analytic Tower of serial connection,
1) process furnace and the reactor of two groups of parallel connections of employing, cyclical operation;
2) in the reactor, processing condition are: 320～420 ℃ of temperature of reaction, and pressure 0.8～2.0MPa, mass space velocity are 0.4～0.8h-1, the mass ratio of light hydrocarbon component and low octane value gasoline is 30: 70～10: 90;
3) the interior light hydrocarbon component of reactor is a kind of or its mixture in catalysis drying gas, coking dry gas or the catalytic coking liquefied gas; Described low octane value gasoline is a kind of or its arbitrary combination in straight-run spirit, field condensate, hydrotreated naphtha, the pyrolysis gasoline of often reducing pressure;
4) serial connection stabilizer tower and weight-removing column behind the described absorption Analytic Tower.
2. the method that refinery gas according to claim 1, lighter hydrocarbons are produced the stop bracket gasoline blend component, it is characterized in that, a light hydrocarbon component part is with after low octane value gasoline mixes, after being heated to 320～420 ℃, process furnace enters reactor, remainder enters second and third bed of reactor after the evaporating heater vaporization.
3. a refinery gas, lighter hydrocarbons are produced the device of stop bracket gasoline blend component, it is characterized in that,
Comprise first process furnace, first reactor, the first reactor bottom discharge nozzle is successively through the first reaction product interchanger, the first reaction product aftercooler, and serial connection absorbs Analytic Tower, stabilizer tower and weight-removing column successively then;
Comprise that also second process furnace and second reactor and first process furnace, first reactor are in parallel, the second reactor bottom discharge nozzle is successively through the second reaction product interchanger, the second reaction product aftercooler, and serial connection absorbs Analytic Tower, stabilizer tower and weight-removing column successively then;
The light hydrocarbon component fresh feed pump is connected first process furnace, second process furnace respectively with behind the first reaction product interchanger, the second reaction product interchanger with the gasoline feeding pump, enters first reactor and the second reactor head feed-pipe then respectively;
First, second reactor with burn jar, recycle gas compressor and the circulation of first, second reaction product interchanger be connected, also is provided with evacuation burning on jar and the recycle gas compressor connecting pipeline.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104152177A (en) * | 2014-08-19 | 2014-11-19 | 山东利丰达生物科技有限公司 | Aromatization method for liquefied gas |
| CN105861039A (en) * | 2015-01-23 | 2016-08-17 | 上海优华系统集成技术有限公司 | liquefied gas aromatization apparatus |
| CN106520190A (en) * | 2016-12-14 | 2017-03-22 | 四川中腾能源科技有限公司 | Light hydrocarbon production method |
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| CN1320677A (en) * | 2001-02-28 | 2001-11-07 | 王凤阳 | Process for regenerating secondary catalyst in oil refinery |
| CN1600836A (en) * | 2003-09-28 | 2005-03-30 | 中国石油化工股份有限公司 | Method for preparing gasoline with low content of olefin by modifying direct distillation gasoline |
| CN1814713A (en) * | 2005-01-31 | 2006-08-09 | 中国科学院大连化学物理研究所 | Catalytic convertion method of liquified petroleum gas and gasoline feeding at same time |
| CN101333461A (en) * | 2008-03-25 | 2008-12-31 | 北京惠尔三吉绿色化学科技有限公司 | Method for producing cleaning fuel oil form petroleum cracking dry gas and C4 component |
| CN101429452A (en) * | 2007-11-08 | 2009-05-13 | 中国石油天然气股份有限公司 | Method for producing high-octane gasoline |
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2011
- 2011-05-10 CN CN2011101191712A patent/CN102226102A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1320677A (en) * | 2001-02-28 | 2001-11-07 | 王凤阳 | Process for regenerating secondary catalyst in oil refinery |
| CN1600836A (en) * | 2003-09-28 | 2005-03-30 | 中国石油化工股份有限公司 | Method for preparing gasoline with low content of olefin by modifying direct distillation gasoline |
| CN1814713A (en) * | 2005-01-31 | 2006-08-09 | 中国科学院大连化学物理研究所 | Catalytic convertion method of liquified petroleum gas and gasoline feeding at same time |
| CN101429452A (en) * | 2007-11-08 | 2009-05-13 | 中国石油天然气股份有限公司 | Method for producing high-octane gasoline |
| CN101333461A (en) * | 2008-03-25 | 2008-12-31 | 北京惠尔三吉绿色化学科技有限公司 | Method for producing cleaning fuel oil form petroleum cracking dry gas and C4 component |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104152177A (en) * | 2014-08-19 | 2014-11-19 | 山东利丰达生物科技有限公司 | Aromatization method for liquefied gas |
| CN104152177B (en) * | 2014-08-19 | 2016-03-16 | 山东利丰达生物科技有限公司 | A kind of method of liquefied gas through aromatization |
| CN105861039A (en) * | 2015-01-23 | 2016-08-17 | 上海优华系统集成技术有限公司 | liquefied gas aromatization apparatus |
| CN106520190A (en) * | 2016-12-14 | 2017-03-22 | 四川中腾能源科技有限公司 | Light hydrocarbon production method |
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Application publication date: 20111026 |