CN108795490A - It reforms full fraction and generates oily hydrogenation plant and cut light tower coupled system - Google Patents
It reforms full fraction and generates oily hydrogenation plant and cut light tower coupled system Download PDFInfo
- Publication number
- CN108795490A CN108795490A CN201710306523.2A CN201710306523A CN108795490A CN 108795490 A CN108795490 A CN 108795490A CN 201710306523 A CN201710306523 A CN 201710306523A CN 108795490 A CN108795490 A CN 108795490A
- Authority
- CN
- China
- Prior art keywords
- hydrogenation
- heat exchanger
- hydrogenation plant
- pipeline
- cut light
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of full fractions of reformation to generate oily hydrogenation plant and cut light tower coupled system, including：Hydrogenation plant and cut light tower, cut light tower include boiling system again, specifically include delivery pump, reboiler furnace and supporting pipelines and control system；Hydrogenation plant and cut light tower coupled relation, the heat exchanger A being arranged on pipeline is removed including hydrogenation products, bottom of tower heavy constituent removes the heat exchanger B being arranged on pipeline, hydrogenation products remove pipeline and are connected to heat exchanger A, it is connected to again with heat exchanger B through pipeline, hydrogenation products remove pipeline, and most the feeding line through cut light tower is connected to cut light tower afterwards.In prior art basis, solve the problems, such as that hydrogenation plant temperature is promoted to operate cut light tower influences the present invention, is conducive to device steady running and extends operation cycle.
Description
Technical field
The complete oily hydrogenation plant of fraction generation and cut light tower coupled system are reformed the present invention relates to a kind of, specifically
A kind of system of the reforming reaction liquid product liquid-phase hydrogenatin removing containing carbon-carbon double bond and/or triple carbon-carbon bonds hydro carbons.
Background technology
Catalytic reforming（Catalytic Reforming）It is one of petroleum refining main process.It is in certain temperature, pressure
Power under the conditions of facing existing for hydrogen and catalyst, makes naphtha be transformed into the reforming reaction liquid product rich in aromatic hydrocarbons, and coproduct hydrogen
The process of gas.Reforming reaction liquid product can be directly used as the blend component of motor petrol, and benzene, first can be also produced through Aromatics Extractive Project
The hydrogen of one of benzene and dimethylbenzene, by-product is oil plant hydrogenation plant（Such as hydrofinishing is hydrocracked) with hydrogen it is main come
One of source.
Since first set hydroforming process device in 1940 is gone into operation, catalytic reforming process is so far after nearly more than 60 years
Development course, the demand with market and human lives to fuel and aromatic hydrocarbons, many countries are all continuous to catalytic reforming process
R and D are carried out.
The development of catalytic reforming process should include two parts：That is the development of catalytic reforming process and catalytic reforming catalyst
Development, the two complements each other, indispensable.Catalytic reforming catalyst determines the rate and depth of catalytic reforming reaction process
Degree is to determine that most important factor during catalytic reforming process, the development of catalytic reforming catalyst support catalytic reforming again
The development of technique.Conversely, the development of catalytic reforming process, and push the further R and D of catalytic reforming catalyst.
In recent years, with the development of reforming catalyst and catalytic reforming process, in addition adverse current vertical heat exchanger, multithread road
The introducing of the high-efficiency appliances such as combination furnace, improves technological process, reduces the pressure drop for facing hydrogen system, catalytic reforming
Face hydrogen pressure to be greatly reduced；Energy consumption is also reduced simultaneously, improves product yield.Due to reformer reaction pressure
It further decreases, reacts further increasing for severity, cause to be rich in a large amount of unsaturated hydrocarbons in reforming reaction liquid product, such as
The hydro carbons for having carbon-carbon double bonds or triple carbon-carbon bonds seriously affects follow-up aromatic extraction unit stable operation and product quality.Therefore
Reforming reaction liquid product is usually pre-processed before entering Aromatics Extractive Project.China still has a large amount of reformers to adopt at present
With active earth pretreatment technique.That there is refining depths is poor for active earth pretreatment technique, heavy constituent yield is big, carclazyte inactivation is fast etc. asks
There is serious risk of environmental pollution for topic, the especially disposition of inactivation spent bleaching clay, and Petrochemical Enterprises is made to face huge environmental protection pressure
Power.
In recent years, the related of technology of alkene is reported in external existing selective hydrogenation and removing reforming reaction liquid product
It leads（The Arofining techniques of French IFP）.Using the benzene fraction of reforming reaction liquid product as raw material, using noble metal catalyst,
Alkene under conditions of comparing mitigation in removing raw material.Both at home and abroad there is not yet catalytic reforming reaction liquid product BTX fractions and
The commercial Application report of full fraction selective hydrogenation and olefin hydrocarbon removal technology.
China Petroleum and Chemical Corporation Fushun Petrochemical Research Institute develops to be carried out using noble metal catalyst
Catalytic reforming reaction liquid product selective hydrogenation and olefin hydrocarbon removal technology（FHDO）.FHDO technologies are successfully applied in Maoming stone within 2003
On the benzene fraction hydrogenation and olefin hydrocarbon removal device for changing branch company；2005 successfully in Yanshan Mountain BTX fractions selective hydrogenation and olefin hydrocarbon removal and
Chang Ling branch company BTX fraction selective hydrogenation and olefin hydrocarbon removal commercial plants realize commercial Application；It is reformed in Zhenghai refinery within 2009 anti-
It answers and realizes commercial Application on the full fraction selective hydrogenation and olefin hydrocarbon removal commercial plant of liquid product.The reforming reaction of commercial Application at present
Liquid product selective hydrogenation and olefin hydrocarbon removal device is equipped with the dynamic equipment such as raw material pump, make-up hydrogen compressor, circulating hydrogen compressor, device
Hydrogen circulate operation.The cycle of hydrogen not only brings the higher energy consumption of device, while also forming Wen Sheng in reactor, makes
At the fractional saturation of aromatic hydrocarbons, the economic benefit of enterprise is affected.
CN103666544B discloses a kind of recapitalization generating oil hydrogenation processing method, and this method is included in liquid-phase hydrogenatin processing
Under the conditions of, reformed oil is contacted with the catalyst with catalytic hydrogenation in hydrogenation reactor, described plus hydrogen
The hydrogen used in processing is directly entered de- at least partially from the dissolved hydrogen in the reformed oil, hydrogenation reaction product
Lights column.According to this method, isolated reformed oil from reformate knockout drum is directly subjected to liquid-phase hydrogenatin
Processing, takes full advantage of the dissolved hydrogen in reformed oil, and device constitutes simple.It has the following disadvantages in practice：（1）In order to
Strengthen liquid-phase hydrogenatin reaction, what it is into hydrogenation reactor is reformed oil isolated in reformate knockout drum, ability
Field technique personnel know, still contain more light hydrocarbon component in reformate knockout drum in isolated gas phase, and this method needs
It wants other devices to recycle the light hydrocarbon component, does not make full use of reforming system device and working condition；（2）It is de- light in order to meet
The temperature requirement of component tower charging, the temperature of hydrogenation reaction device are only capable of adjusting in smaller range, in general cannot be satisfied and urge
Agent activity promotes temperature to reach the requirement of required reaction depth after declining.CN203878113U discloses a kind of reforming reaction
Liquid product hydrogenation system.The system includes hydrogenation reactor, hydrogenation reactor setting reform contactor again and stabilizer it
Between, the high-purity hydrogen that is obtained using contactor again is carried out online with after contactor bottom of tower oil mixes again in hydrogenation reactor
Liquid-phase hydrogenatin is reacted, and reaction product enters back into stabilizer.The system can be under the process conditions more mitigated, to reforming reaction
Liquid product carries out depth-selectiveness hydrogenation reaction；It, can be straight since hydrogenation reactor setting is again between contactor and stabilizer
The hydrogen obtained using contactor again is connect as hydrogen source, hydrogenation and removing carbon-carbon double bonds or carbon carbon are carried out under the conditions of liquid-phase hydrogenatin
The reaction of three key hydro carbons significantly reduces cost of investment and behaviour to eliminate the circulating hydrogen compressor in existing hydrogenation system
Make cost.The deficiency of the system is：Hydrogenation reaction product is directly entered cut light tower, therefore hydrogenation reaction temperature is by de- light
The limitation of component tower feeding temperature, cannot adjust on a large scale, and the required reaction temperature to adapt to catalyst activity variation adjusts.
Invention content
Technical problem to be solved by the present invention lies in, provide it is a kind of reform full fraction generate oily hydrogenation plant with it is light group de-
Divide tower-coupled system, for carrying out that hydrogen is added to remove carbon-carbon double bonds and/or triple carbon-carbon bonds to catalytic reforming reaction liquid product
Hydrocarbon impurities contain carbon-carbon double bonds in catalytic reforming reaction liquid product or triple carbon-carbon bonds hydro carbons with meeting aromatic extraction unit
The limitation of amount, while hydrogenation reaction device reaction temperature can need to be adjusted in wide range according to reaction, while not
Influence the normal operating of the cut light tower coupled with hydrogenation plant.
Technical solution provided by the invention is：
It is a kind of to reform full fraction and generate oily hydrogenation plant and cut light tower coupled system, including：
Hydrogenation plant comprising for hydrogenation plant charging to be led to the feeding line of the hydrogenation reaction device, and for moving
The hydrogenation products for going out hydrogenation products remove pipeline；
Cut light tower comprising for cut light tower charging is led to the feeding line of the cut light tower, and be used for
The removal pipeline of the tower top light component obtained after fractionation is removed, and for removing the removal of the bottom of tower heavy constituent obtained after fractionation
Pipeline；Further include boiling system again, specifically includes delivery pump, reboiler furnace and supporting pipelines and control system；
Hydrogenation plant includes with cut light tower coupled relation：Heat riser and temperature control are set on hydrogenation plant feeding line
Device, for regulating and controlling hydrogenation plant reaction temperature, heat riser is heat exchanger C, and exchanger heat logistics is to boil system delivery pump again
At least part of outlet material, i.e. delivery pump outlet line are connected to heat exchanger C heated stream entrances, and heat exchanger C heats object
Outflux is connected to reboiler furnace entrance, and reboiler furnace outlet is boiled material inlet with cut light tower and is connected to again.Preferably, in heat exchanger
Cross-line is set between C heated streams entrance and outlet, flow regulator is set on cross-line, to adjust into heat exchanger C's
Logistics flux.
Hydrogenation plant further preferably includes with cut light tower coupled relation comprising hydrogenation products, which remove, to be arranged on pipeline
Heat exchanger A（Cool down to hydrogenation products）, bottom of tower heavy constituent removes the heat exchanger B that is arranged on pipeline（It heats up to hydrogenation products）, add
Hydrogen product removes pipeline and is connected to heat exchanger A, then is connected to heat exchanger B through pipeline, and hydrogenation products remove pipeline most afterwards through de- light
The feeding line of component tower is connected to cut light tower.
In the present invention, the cold material of heat exchanger A feeds for hydrogenation plant, and the thermal material of heat exchanger B is cut light tower
Bottom of tower heavy constituent.
In the present invention, pre- hydrogenation plant can be set before hydrogenation plant, operated at the temperature lower than hydrogenation plant, in advance
Hydrogenation plant outlet line is connected to heat exchanger A, is reformed full fraction liquid product and is first passed through progress pre-add hydrogen in pre- hydrogenation plant,
Then it carries out adding hydrogen in hydrogenation plant.
In the present invention, hydrogen make pipeline and hydrogen amount control device, supplement is arranged in hydrogenation plant and/or pre- hydrogenation plant
Amounts of hydrogen determines according to reaction requirement, but using not to cut light tower behaviour as premised on generating and seriously affect.It can be arranged
Air and liquid mixer adds to hydrogen make-up in hydrogenation plant charging, can also be mixed by pipeline or by other existing apparatus
（Such as heat exchanger）Auxiliary mixing.
In the present invention, reforms full fraction liquid product and generally comprise and recycled reformer lighter hydrocarbons（Reform hydrogen in lighter hydrocarbons,
Lighter hydrocarbons etc. in cut light tower tower overhead gas）, supplemented with the Suitable base in other sources.It can be arranged as required to connect again
Tentaculum（Reformed oil contacts again with hydrogen is reformed, and recycles lighter hydrocarbons therein）, removing impurities matter tank（Such as dechlorination tank）, liquefied gas restoring
Existing way may be used in tank etc., specific set-up mode, as described in CN203878113U etc..
In the present invention, hydrogenation plant or pre- hydrogenation plant it is preferable to use noble metal catalyst, catalyst generally with Pt and/or
Pt is active component, and carrier is generally aluminium oxide.Hydrogenation plant feeding manner can be upper feeding, can also be lower charging.
In the present invention, hydrogenation plant may include more than two catalyst beds.It is preferred that further include with dealing two with
The feeding line of arbitrary source hydrogen is supplemented between upper catalyst bed.
In the present invention, hydrogen make-up can be to reform the appropriate high-purity hydrogen that contactor obtains again, can also be other
The hydrogen in source.
In the present invention, air and liquid mixer can be static mixer or dynamic mixer, preferably static mixer.Static state is mixed
Clutch can be selected from SV types static mixer, SK types static mixer, SX types static mixer, SH types static mixer, SL types
One or several kinds of combinations in static mixer, dynamic mixer can be selected from mixing pump, overcritical mixer, be stirred
One or several kinds of combinations in device.
In the present invention, it can also include catalytic reforming reaction product gas-liquid separator, wherein produce catalytic reforming reaction
Object is separated into hydrogen-rich gas and reforming reaction liquid product.Gas-liquid separator includes being fed catalytic reforming reaction product with dealing
To the feeding line of the gas-liquid separator, the pipeline for removing hydrogen-rich gas, the increasing for being pressurized to hydrogen-rich gas
Pressure compressor, the pipeline for removing reforming reaction liquid product and the pump for being pressurized to reforming reaction solution phase product.
Wherein, for feeding catalytic reforming reaction product cooling is being usually provided on the feeding line to the gas-liquid separator
Device, for being cooled down to catalytic reforming reaction product.
The reformation is again in contactor, for by hydrogen-rich gas after supercharged and reforming reaction liquid phase after supercharged production
Object is fed to cooler is usually also set up on the feeding line of contactor again, to further decrease the temperature of mixed feeding, is obtained
Better lighter hydrocarbons recovery effect and the purity for improving hydrogen.
In the present invention, on the feeding line fed the mixed material from air and liquid mixer to hydrogenation reactor usually
Heat riser can also be set, and it is anti-that hydrogen and the again mixed feeding of contactor bottom of tower oil by heat riser are heated to hydrogen
Answer the inlet temperature of device.Alternatively, the hydrogen in arbitrary source can fed with contactor bottom of tower oil is reformed again to gas-liquid mixed
Heat riser is set on the feeding line of device, after hydrogen and bottom of tower oil are preheated to reactor inlet temperature, enters back into gas
Liquid mixer carries out molten hydrogen.
In the present invention, hydrogenation plant reaction product gas-liquid separator can be set, the gas phase and liquid phase after separation respectively from
Suitable position introduces cut light tower.
In the present invention, the operation temperature of pre- hydrogenation plant is generally below 10~100 DEG C of hydrogenation plant.
Compared with prior art, the invention has the advantages that：
1, hydrogenation system of the invention can carry out depth choosing under the process conditions more mitigated to reforming reaction solution phase product
Selecting property adds hydrogen, with remove carbon-carbon double bonds therein and/or or triple carbon-carbon bonds hydro carbons, aromatic hydrocarbons loss amount can be in hydrogenation process
It controls at 0.5 percentage point hereinafter, the reforming reaction liquid product after therefore adding hydrogen can meet downstream Aromatics Extractive Project dress completely
Set the quality requirement to charging.
2, since hydrogenation reactor setting between contactor and stabilizer, can obtained directly using contactor again again
Appropriate amount of hydrogen carries out adding hydrogen under the conditions of liquid-phase hydrogenatin, eliminates the circulating hydrogen compressor in existing hydrogenation system as hydrogen source,
Reduce cost of investment and operating cost.
3, since hydrogenation reactor setting between contactor and stabilizer, is reducing raw material heating and cooling process again, thus
The low level heat source that device can be taken full advantage of reduces the operation energy consumption of device.
4, reaction environment is mainly liquid phase reactor in hydrogenation reactor, has cut down the probability of bias current and channel appearance, has made dress
The reforming reaction liquid product property being refining to obtain is set more to stablize.
5, due in device separator hydrogen be unsaturated state, reduce disappearing for enterprise's hydrogen loss or hydrogen recycling
Consumption, also reduces plant energy consumption.
6, it is combined with hydrogenation plant using pre- hydrogenation plant, the low temperature active and high temperature of hydrogenation catalyst can be made full use of
Activity is conducive to extend the service life of catalyst.
7, by the coupled relation of hydrogenation plant and cut light tower, it ensure that hydrogenation plant adjusts temperature in wide range
When spending, the operation of cut light tower is influenced smaller.Hydrogenation plant reaction product is first cooled down the heat exchange stream to heat up afterwards
Journey can ensure that the fluctuation of cut light tower inlet temperature is smaller although theoretically heating efficiency decreases.It is computed
When showing that hydrogenation plant reaction temperature adjusts within the scope of 100~230 DEG C, cut light tower inlet temperature fluctuation range is at 5 DEG C
It controls, and be macrocyclic slow fluctuation not influencing its normal operating by the simple adjustment of cut light tower.When operation
The operation of cut light tower is influenced without worry adjustment temperature of reactor.Under being discharged to outside the bottom of tower heavy constituent of cut light tower
Before one processing unit（Or in next processing unit）Temperature of charge regulator control system is set, meets next processing unit to material
The demand of temperature, so that it may so that this system and the operating of downstream processing unit automatic steady, are not required to excessive artificial adjusting.
8, the lighter hydrocarbons of reforming process recycle in the device, are not required to that light ends unit is separately arranged.
9, it is big to boil system mass flow again for cut light tower, has power plant, the temperature tune for hydrogenation plant charging
The whole adjustment space with bigger, higher adjustment flexibility, is conducive to commercial plant stable operation.Cut light tower is boiled again
System has a heating furnace, and the advantage of heating furnace is to adjust sensitive, is influenced by charging smaller, therefore, above-mentioned adjustment does not influence light group de-
Divide the stable operation of tower.
Description of the drawings
Fig. 1 is a kind of composition schematic diagram of the present invention.
Fig. 2, which is that the present invention is another, constitutes schematic diagram.
Specific implementation mode
The reforming reaction liquid product hydrogenation system of the present invention is carried out in the following with reference to the drawings and specific embodiments detailed
Description.
As shown in Figure 1, the present invention includes：Reform contactor 12 again comprising for feeding hydrogen-rich gas after supercharged
To the feeding line 9 of contactor again and reforming reaction liquid product after supercharged is fed to the charging of the contactor again
Pipeline 8 removes pipeline 13 and for removing again the removal pipeline 14 that contactor generates oil for removing the hydrogen of hydrogen.
The reformation is again in contactor 12, for by hydrogen-rich gas after supercharged feed to the contactor again into
It is additionally provided with cooler 11 on expects pipe line 9, reforming reaction liquid product after supercharged is fed to the charging of the contactor again
Cooler 10 can also be set on pipeline 8, further decrease the temperature of charging, returned with obtaining better lighter hydrocarbons in contactor again
Produce effects fruit and improve hydrogen purity.
Air and liquid mixer 15 comprising for will be fed to the air and liquid mixer from the bottom of tower oil for reforming again contactor
Feeding line 14, for feeding the hydrogen from arbitrary source to the feeding line of the air and liquid mixer.Such as Fig. 1 institutes
Show, in the present embodiment, for feeding the hydrogen from arbitrary source to the feeding line of air and liquid mixer and reforming again
The hydrogen removal pipeline 13 for being used for removing hydrogen in contactor is connected, i.e., the hydrogen in the arbitrary source can be to reform again
The appropriate high-purity hydrogen that contactor obtains.According to the structure of air and liquid mixer, hydrogen can be introduced directly into air and liquid mixer,
Air and liquid mixer can also be entered after other positions are mixed with raw material.
Hydrogenation reactor 18 comprising for feeding the mixed material from air and liquid mixer to the hydrogenation reactor
Feeding line 17, and for remove hydrogenation products hydrogenation products remove pipeline 19.
Hydrogenation reactor 18 generally includes more than two hydrogenation catalyst beds 24.The hydrogenation system preferably also wraps
It includes with supplement hydrogen feeding line of the supplement from arbitrary source hydrogen between dealing two or more catalyst bed.In this embodiment party
In formula, with the supplement hydrogen feeding line and reformation for supplementing the hydrogen from arbitrary source between dealing two or more catalyst bed
Again in contactor be used for remove hydrogen hydrogen remove pipeline 13 be connected, you can with using reform again contactor obtain it is appropriate
High-purity hydrogen is as supplement hydrogen.
The hydrogenation reactor 18 is liquid phase hydrogenation reactor（Predominantly liquid phase, small part are the gas of material gasification
Phase）, can be upper feeding or lower charging reactor, lower charging reactor is preferably used in the present invention.
In the hydrogenation reactor 18, by the mixed material from air and liquid mixer feed to hydrogenation reactor into
Heat riser 16.3 is preferably provided on expects pipe line 17（Heat exchanger C）, it is used for hydrogen and the mixed feeding of contactor bottom of tower oil again
The inlet temperature of hydrogenation reactor is heated to by heat riser.Alternatively, as needed can be will be from the hydrogen of contactor again
Gas and bottom of tower oil are fed to heat riser is arranged on the feeding line of air and liquid mixer.Heat riser is heat exchanger form, heat exchange
The hot logistics of device is to boil at least part of 31 outlet material of system delivery pump again, i.e., 31 outlet line of delivery pump is heated with heat exchanger
Stream inlet is connected to, and the outlet of heat exchanger heated stream is connected to 32 entrance of reboiler furnace, and the outlet of reboiler furnace 32 and cut light tower are again
Boil material inlet connection.Preferably, cross-line is set between heat exchanger heated stream entrance and outlet, flow is set on cross-line
Regulating device, to adjust the logistics flux into heat exchanger.
Further include gas-liquid separator 3 in the present invention comprising fed catalytic reforming reaction product to the gas with dealing
The feeding line 1 of liquid/gas separator 3, the pipeline 4 for removing hydrogen-rich gas, the booster compression for being pressurized to hydrogen-rich gas
Machine 5, the pipeline 6 for removing reforming reaction liquid product and the pump 7 for being pressurized to reforming reaction solution phase product.Its
In, it is being additionally provided with cooler 2 on the feeding line 1 to the gas-liquid separator 3 for feeding catalytic reforming reaction product,
For being cooled down to catalytic reforming reaction product.
In the present invention, cut light tower 20（Also referred to as stabilizer）Comprising it is used for liquid phase hydrogenation reactor hydrogenation products
It feeds to the feeding line 19 of the cut light tower, the hydrogenation products as hydrogenation reactor 18 remove the feeding line simultaneously
Pipeline, the overhead product for removing cut light tower overhead gas product remove pipeline 21 and for producing reforming reaction liquid phase
The removal pipeline 22 that object is discharged from cut light tower.
In the present invention, hydrogenation reactor discharges first in heat exchanger 16.1（Heat exchanger A）In with hydrogenation reactor charging change
Heat（Cooling）Afterwards, then in heat exchanger 16.2（Heat exchanger B）In with cut light tower bottom of tower discharge exchange heat（Heating）, subsequently into de-
Lights column carries out fractionation processing.Hydrogenation reactor discharging by first cool down afterwards heat up adjustment, meet de- light component well
The requirement that tower feeding temperature is stablized.If without the adjustment of cooling, heating heat exchange, cut light tower feeding temperature are directly carried out
It can be improved with the raising of hydrogenation reactor temperature, the final normal operating for influencing cut light tower.
Fig. 2 show the composition schematic diagram of another specific implementation mode of the invention.Wherein chief component is the same as in Fig. 1
Flow, repeat no more.
Wherein difference place be, before hydrogenation reactor be arranged pre-hydrogenator 23, pre-hydrogenator 23 into
Material carries out pre-hydrotreating reaction after the heating of heat exchanger 16.4, and the thermal material of heat exchanger 16.4 can be suitable hot logistics, such as
It exchanges heat by heat exchanger 16.2（Cooling）Cut light tower bottom of tower discharge material etc..
In conjunction with Fig. 1, the present invention adds a kind of technical process of hydrogen to be for reforming reaction liquid product：
Reforming reaction product from reforming reactor is detached after pipeline 1, cooler 2 into gas-liquid separator 3, at it
It is middle to pass through isolated hydrogen-rich gas and reforming reaction liquid product.3 gained hydrogen-rich gas of gas-liquid separator enters through pipeline 4 to be increased
Pressure compressor 5 is pressurized, and gained reforming reaction liquid product enters pump 7 through pipeline 6 and is pressurized.Hydrogen-rich gas after supercharged
Through pipeline 9 and cooler 11, reforming reaction liquid product after supercharged respectively enters reformation again after pipeline 8 and cooler 10
Contactor 12 further removes the lighter hydrocarbons contained in hydrogen-rich gas.It reforms again contactor 12 and obtains the hydrogen of high-purity through hydrogen
Pipeline 13 is removed to remove, all the way through pipeline with after by the reformation of pipeline 14, contactor bottom of tower oil mixes again by heating up, gas-liquid
Mixer 15 and pipeline 17, or by air and liquid mixer 15 and heat up after through pipeline 17 enter hydrogenation reactor 18, with containing
The hydrogenation catalyst contact of active component platinum carries out liquid-phase hydrogenatin reaction, removes in reforming reaction liquid product and contains carbon-carbon double bond
And/or the hydrocarbon impurities of triple carbon-carbon bonds；The another way for reforming the high-purity hydrogen that contactor obtains again enters recycle hydrogen through pipeline
More than two hydrogenation catalysts that third road hydrogen enters hydrogenation reactor 18 by pipeline can be arranged in compressor or separating device
Between agent bed 24, it is used as supplement hydrogen.The hydrogenated product of hydrogenation reaction product removes pipeline 19 and first passes through the cooling of heat exchanger 16.1,
Entering stabilizer 20 after heat exchanger 16.2 heats up after again, obtained gaseous product removes pipeline 21 by overhead product and is discharged,
The reforming reaction liquid product for obtaining impurity content reduction is discharged through pipeline 22.
Schematic diagram is constituted by Fig. 1 and carries out flowsheeting calculating, when the reaction temperature of hydrogenation reactor 18 is anti-from hydrogenation plant
When temperature being answered to be adjusted within the scope of 130~220 DEG C, cut light tower inlet temperature gradually rises to 191 DEG C from 186 DEG C, by de-
The simple adjustment of lights column, does not influence its normal operating.
Claims (10)
1. a kind of full fraction of reformation generates oily hydrogenation plant and cut light tower coupled system, including：
Hydrogenation plant comprising for hydrogenation plant charging to be led to the feeding line of the hydrogenation reaction device, and for moving
The hydrogenation products for going out hydrogenation products remove pipeline；
Cut light tower comprising for cut light tower charging is led to the feeding line of the cut light tower, and be used for
The removal pipeline of the tower top light component obtained after fractionation is removed, and for removing the removal of the bottom of tower heavy constituent obtained after fractionation
Pipeline；Further include boiling system again, specifically includes delivery pump, reboiler furnace and supporting pipelines and control system；
Hydrogenation plant includes with cut light tower coupled relation：Heat riser and temperature control are set on hydrogenation plant feeding line
Device, for regulating and controlling hydrogenation plant reaction temperature, heat riser is heat exchanger C, and exchanger heat logistics is to boil system delivery pump again
At least part of outlet material, i.e. delivery pump outlet line are connected to heat exchanger C heated stream entrances, and heat exchanger C heats object
Outflux is connected to reboiler furnace entrance, and reboiler furnace outlet is boiled material inlet with cut light tower and is connected to again.
2. system according to claim 1, it is characterised in that：The cold material of heat exchanger A feeds for hydrogenation plant, heat exchanger
The thermal material of B is the bottom of tower heavy constituent of cut light tower.
3. system according to claim 1, it is characterised in that：Pre- hydrogenation plant is set before hydrogenation plant, than adding hydrogen
It is operated at the low temperature of device, pre- hydrogenation plant outlet line is connected to heat exchanger A.
4. system according to claim 3, it is characterised in that：Hydrogen make is arranged in hydrogenation plant and/or pre- hydrogenation plant
Pipeline and hydrogen amount control device.
5. system according to claim 4, it is characterised in that：Air and liquid mixer is set, will be supplemented by air and liquid mixer
During hydrogen make is fed to hydrogenation plant.
6. system according to claim 3, it is characterised in that：Hydrogenation plant or pre- hydrogenation plant use precious metal catalyst
Agent, for catalyst using Pt and/or Pt as active component, carrier is aluminium oxide.
7. system according to claim 1, it is characterised in that：Hydrogenation plant reaction product gas-liquid separator, separation are set
Gas phase and liquid phase afterwards introduces cut light tower from suitable position respectively.
8. system according to claim 3, it is characterised in that：The operation temperature of pre- hydrogenation plant less than hydrogenation plant 10~
100℃。
9. system according to claim 1, it is characterised in that：It is arranged between heat exchanger C heated streams entrance and outlet
Flow regulator is arranged in cross-line on cross-line, to adjust the logistics flux into heat exchanger C.
10. system according to claim 1, it is characterised in that：Hydrogenation plant further includes with cut light tower coupled relation：
It includes that hydrogenation products remove the heat exchanger A being arranged on pipeline, and bottom of tower heavy constituent removes the heat exchanger B being arranged on pipeline, adds hydrogen
Product removes pipeline and is connected to heat exchanger A, then is connected to heat exchanger B through pipeline, and hydrogenation products remove pipeline most afterwards through light group de-
The feeding line of tower is divided to be connected to cut light tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710306523.2A CN108795490B (en) | 2017-05-04 | 2017-05-04 | Coupling system of hydrogenation device and light component removal tower for reforming full distillate generated oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710306523.2A CN108795490B (en) | 2017-05-04 | 2017-05-04 | Coupling system of hydrogenation device and light component removal tower for reforming full distillate generated oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108795490A true CN108795490A (en) | 2018-11-13 |
| CN108795490B CN108795490B (en) | 2023-07-28 |
Family
ID=64054275
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710306523.2A Active CN108795490B (en) | 2017-05-04 | 2017-05-04 | Coupling system of hydrogenation device and light component removal tower for reforming full distillate generated oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108795490B (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0127284A1 (en) * | 1983-04-26 | 1984-12-05 | Mobil Oil Corporation | Exothermic hydrocarbon conversion system utilizing heat exchange between reactor effluent fractionation system and feedstock |
| US20060118466A1 (en) * | 2001-11-22 | 2006-06-08 | Renaud Galeazzi | Two-step method for hydrotreating of a hydrocarbon feedstock comprising intermediate fractionation by rectification stripping |
| CN203878113U (en) * | 2014-05-25 | 2014-10-15 | 中国石油化工股份有限公司 | Reforming reaction liquid-phase product hydrogenation system |
| CN105670689A (en) * | 2016-02-01 | 2016-06-15 | 北京燕山玉龙石化工程有限公司 | Kerosene-hydrogenation production process and system |
| CN206768032U (en) * | 2017-05-04 | 2017-12-19 | 中国石油化工股份有限公司抚顺石油化工研究院 | Reform full cut and generate oily hydrogenation plant and cut light tower coupled system |
-
2017
- 2017-05-04 CN CN201710306523.2A patent/CN108795490B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0127284A1 (en) * | 1983-04-26 | 1984-12-05 | Mobil Oil Corporation | Exothermic hydrocarbon conversion system utilizing heat exchange between reactor effluent fractionation system and feedstock |
| US20060118466A1 (en) * | 2001-11-22 | 2006-06-08 | Renaud Galeazzi | Two-step method for hydrotreating of a hydrocarbon feedstock comprising intermediate fractionation by rectification stripping |
| CN203878113U (en) * | 2014-05-25 | 2014-10-15 | 中国石油化工股份有限公司 | Reforming reaction liquid-phase product hydrogenation system |
| CN105670689A (en) * | 2016-02-01 | 2016-06-15 | 北京燕山玉龙石化工程有限公司 | Kerosene-hydrogenation production process and system |
| CN206768032U (en) * | 2017-05-04 | 2017-12-19 | 中国石油化工股份有限公司抚顺石油化工研究院 | Reform full cut and generate oily hydrogenation plant and cut light tower coupled system |
Non-Patent Citations (1)
| Title |
|---|
| 李国庆: "炼油过程分馏和换热系统能量优化研究" * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108795490B (en) | 2023-07-28 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN203878113U (en) | Reforming reaction liquid-phase product hydrogenation system | |
| TW201114884A (en) | Process for regenerative reforming of gasolines, comprising recycling at least a portion of the effluent from the catalyst reduction phase | |
| CN103396833B (en) | A kind of synthetic naphtha produces the method for motor spirit | |
| CN106608805A (en) | C3 fraction liquid phase selective hydrogenation method | |
| RU2295557C2 (en) | Hydrocarbon feedstock catalytic reforming process | |
| CN107207976A (en) | For reforming integrated approach and system with isomerization hydrocarbon | |
| CN206768032U (en) | Reform full cut and generate oily hydrogenation plant and cut light tower coupled system | |
| CN206768035U (en) | Recapitalization generating oil hydrogenation device and cut light tower coupled system | |
| CN206768033U (en) | Reform full cut liquid product hydrogenation plant and cut light tower coupled system | |
| CN206768029U (en) | Reformed oil liquid-phase hydrogenatin device and cut light tower coupled system | |
| CN108795490A (en) | It reforms full fraction and generates oily hydrogenation plant and cut light tower coupled system | |
| CN106753561B (en) | A kind of method of liquefied gas preparing ethylene cracking material by hydrogenation | |
| CN1226227A (en) | Method for producing high purity isobutylene from butane plus fraction containing isobutylene and butylene-1 | |
| CN107304371B (en) | A kind of recapitalization generating oil hydrogenation processing method | |
| CN108795494A (en) | Recapitalization generating oil hydrogenation device and cut light tower coupled system | |
| CN108795491A (en) | Reform full fraction liquid product hydrogenation plant and cut light tower coupled system | |
| CN108795486A (en) | Reformed oil liquid-phase hydrogenatin device and cut light tower coupled system | |
| CN104232151B (en) | A kind of Benzin naphtha catalytic reforming method | |
| CN101376826B (en) | Hydrogenation technological process for long distillate coking kerosene | |
| CN107304376B (en) | A kind of reformed oil liquid-phase hydrogenatin processing method | |
| EP2402417B1 (en) | Method for collecting hydrocarbon compound from gaseous by-product and apparatus for collecting hydrocarbon | |
| CN102465016B (en) | Combined hydrogenation process | |
| CN109722297A (en) | A kind of catalytic reforming process system and process | |
| CN107304372B (en) | A kind of reformed oil liquid-phase hydrogenatin processing method | |
| CN107304369B (en) | A kind of recapitalization generating oil hydrogenation method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |