CN206768035U - Recapitalization generating oil hydrogenation device and cut light tower coupled system - Google Patents

Abstract

The utility model discloses a kind of recapitalization generating oil hydrogenation device 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 includes with cut light tower coupled relation, reboiler furnace outlet sets gas-liquid separator, gas-liquid separator gaseous phase outlet boils material inlet with cut light tower by pipeline and connected again, and gas-liquid separator liquid-phase outlet is connected by pipeline with the heat exchanger B set on cut light tower feeding line.In prior art basis, solve the problems, such as that the lifting of hydrogenation plant temperature operates on cut light tower influences the utility model, is advantageous to device steady running and extends service cycle.

Description

Recapitalization generating oil hydrogenation device and cut light tower coupled system

Technical field

It the utility model is related to a kind of recapitalization generating oil hydrogenation device and cut light tower coupled system, specifically one System of the kind 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, naphtha is set to 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 One of benzene and dimethylbenzene, the hydrogen of by-product is oil plant hydrogenation plant（Such as hydrofinishing, be 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, as market and human lives are continuous to catalytic reforming process to the demand of fuel and aromatic hydrocarbons, many countries 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 speed and depth of catalytic reforming reaction process Degree, it is to determine most important factor during catalytic reforming process, the development of catalytic reforming catalyst supports catalytic reforming again The development of technique.Conversely, the development of catalytic reforming process, promotes the further R and D of catalytic reforming catalyst again.

In the last few years, with the development of reforming catalyst and catalytic reforming process, plus adverse current vertical heat exchanger, more streams 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 Further reduce, react the further raising of severity, cause to be rich in substantial amounts of unsaturated hydrocarbons in reforming reaction liquid product, such as There is the hydro carbons of carbon-carbon double bonds or triple carbon-carbon bonds, have a strong impact on follow-up aromatic extraction unit stable operation and product quality.Therefore Reforming reaction liquid product generally needs to be pre-processed before Aromatics Extractive Project is entered.China still has a large amount of reformers to adopt at present With active earth pretreatment technique.There is refining depth is poor, heavy constituent yield is big, carclazyte inactivates fast etc. ask for active earth pretreatment technique Topic, the disposal of spent bleaching clay is especially inactivated there is serious risk of environmental pollution, Petrochemical Enterprises is faced 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 Lead（French IFP Arofining techniques）.Using the benzene fraction of reforming reaction liquid product as raw material, using noble metal catalyst, Alkene in raw material is removed under conditions of comparing mitigation.Both at home and abroad there is not yet catalytic reforming reaction liquid product BTX cuts and The commercial Application report of full cut 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 cuts selective hydrogenation and olefin hydrocarbon removal and Chang Ling branch company BTX cut selective hydrogenation and olefin hydrocarbon removal commercial plants realize commercial Application；Reformed in Zhenghai refinery within 2009 anti- Answer and realize commercial Application on the full cut 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, provided with the dynamic equipment such as raw material pump, make-up hydrogen compressor, circulating hydrogen compressor, device Hydrogen circulate operation.The circulation of hydrogen, the higher energy consumption of device is not only brought, while temperature rise is also formed in reactor, made Into the fractional saturation of aromatic hydrocarbons, the economic benefit of enterprise have impact on.

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, the hydrogenation 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 forms simple.Have 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 Want other devices to reclaim the light hydrocarbon component, do 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 can not meet to urge Temperature is lifted after agent activity decrease to reach the requirement of required reaction depth.CN203878113U discloses a kind of reforming reaction Liquid product hydrogenation system.The system includes hydrogenation reactor, hydrogenation reactor be arranged on reformation again contactor and stabilizer it Between, after being mixed using the high-purity hydrogen that contactor again obtains with the oil of contactor bottom of towe again, carried out in hydrogenation reactor online Liquid-phase hydrogenatin is reacted, and reaction product enters back into stabilizer.The system can be under the process conditions more relaxed, to reforming reaction Liquid product carries out depth-selectiveness hydrogenation reaction；, can be straight because hydrogenation reactor is arranged on again between contactor and stabilizer Connect by the use of the hydrogen that contactor again obtains 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, so as to eliminate the circulating hydrogen compressor in existing hydrogenation system, significantly reduces cost of investment and behaviour 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, it is impossible to a wide range of adjustment, adjusted with adapting to the required reaction temperature of catalyst activity change.

Utility model content

Technical problem to be solved in the utility model is, there is provided a kind of recapitalization generating oil hydrogenation device and de- light component Tower-coupled system, for being hydrogenated with to catalytic reforming reaction liquid product to remove carbon-carbon double bonds and/or triple carbon-carbon bonds hydrocarbon Class impurity, to meet aromatic extraction unit to carbon-carbon double bonds in catalytic reforming reaction liquid product or triple carbon-carbon bonds hydrocarbon content Limitation, while hydrogenation reaction device reaction temperature can need to be adjusted interior in a big way according to reaction, while not shadow Ring the normal operating of the cut light tower coupled with hydrogenation plant.

Technical scheme provided by the utility model is：

A kind of recapitalization generating oil hydrogenation device and cut light tower coupled system, including：

Hydrogenation plant, it includes the feeding line for hydrogenation plant charging to be led to the hydrogenation reaction device, and use Pipeline is removed to remove the hydrogenation products of hydrogenation products；

Cut light tower, it includes the feeding line for cut light tower charging to be led to the cut light tower, and For removing the removal pipeline of the tower top light component obtained after fractionation, and for removing the bottom of towe heavy constituent obtained after fractionation Remove pipeline；Also include boiling system again, specifically include delivery pump, reboiler furnace and supporting pipelines and control system；

Hydrogenation plant includes with cut light tower coupled relation：Reboiler furnace outlet sets gas-liquid separator, gas-liquid separator Gaseous phase outlet boils material inlet with cut light tower by pipeline and connected again, and gas-liquid separator liquid-phase outlet is light with taking off by pipeline The heat exchanger B connections set on component tower feeding line.

Hydrogenation plant further preferably includes with cut light tower coupled relation：It includes hydrogenation products and removes what is set on pipeline Heat exchanger A（Hydrogenation products are cooled）With heat exchanger B（Hydrogenation products are heated up）, hydrogenation products remove pipeline and heat exchanger A connects It is logical, then connect through pipeline with heat exchanger B, hydrogenation products removal the pipeline most feeding line through cut light tower and de- light component afterwards Tower connects.

Hydrogenation plant further preferably includes with cut light tower coupled relation：Heating is set on hydrogenation plant feeding line Device and temperature control equipment, for regulating and controlling hydrogenation plant reaction temperature, heat riser is heat exchanger C, and exchanger heat logistics is Boiling at least a portion of system delivery pump outlet material again, i.e. delivery pump outlet line connects with heat exchanger C heated stream entrances, The outlet of heat exchanger C heated streams connects with reboiler furnace entrance, and reboiler furnace outlet is boiled material inlet with cut light tower and connected again.It is excellent Selection of land, cross-line is set between heat exchanger C heated streams entrance and outlet, flow regulator is set on cross-line, with regulation Into heat exchanger C logistics flux.

In the utility model, heat exchanger A cold material feeds for hydrogenation plant, and heat exchanger B thermal material is to boil system again Outer row's bottom of towe heavy constituent of the liquid phase material that furnace outlet gas-liquid separator obtains, i.e. cut light tower.

In the utility model, pre- hydrogenation plant can be set before hydrogenation plant, grasped at the temperature lower than hydrogenation plant Make, pre- hydrogenation plant outlet line connect with heat exchanger A, reforms full cut liquid product and first passes through in pre- hydrogenation plant progress in advance Hydrogenation, is then hydrogenated with hydrogenation plant.

In the utility model, hydrogenation plant and/or pre- hydrogenation plant set hydrogen make pipeline and hydrogen amount control device, Hydrogen make-up amount determines according to reaction requirement, but using not to cut light tower behaviour as premised on producing and have a strong impact on.Can be with Set air and liquid mixer to add to hydrogen make-up in hydrogenation plant charging, can also be mixed by pipeline or by other existing Device（Such as heat exchanger）Auxiliary mixing.

In the utility model, reform full cut liquid product and generally comprise and reclaimed reformer lighter hydrocarbons（Reform in hydrogen Lighter hydrocarbons in lighter hydrocarbons, cut light tower tower overhead gas etc.）, supplemented with the Suitable base in other sources.It can set as needed Put contactor again（Reformed oil contacts again with reforming hydrogen, reclaims lighter hydrocarbons therein）, removing impurities matter tank（Such as dechlorination tank）, liquefaction Gas recycling can etc., specific set-up mode can use existing way, as described in CN203878113U etc..

In the utility model, hydrogenation plant or pre- hydrogenation plant preferably use noble metal catalyst, and catalyst is typically with Pt And/or Pt is active component, carrier is generally aluminum oxide.Hydrogenation plant feeding manner can be upper feeding or under enter Material.

In the utility model, hydrogenation plant can include more than two beds.It is preferred that also include using dealing two The feeding line of any source hydrogen is supplemented between individual above beds.

In the utility model, hydrogen make-up can be reform contactor obtains again appropriate high-purity hydrogen or The hydrogen in other sources.

In the utility model, air and liquid mixer can be static mixer or dynamic mixer, preferably static mixer.It is quiet State blender can be selected from SV types static mixer, SK types static mixer, SX types static mixer, SH types static mixer, One or several kinds of combinations in SL type static mixers, dynamic mixer can be selected from mixing pump, overcritical blender, stirring One or several kinds of combinations in blender.

In the utility model, catalytic reforming reaction product gas-liquid separator can also be included, it is wherein that catalytic reforming is anti- Product is answered to be separated into hydrogen-rich gas and reforming reaction liquid product.Gas-liquid separator is included catalytic reforming reaction product with dealing Feed to the feeding line of the gas-liquid separator, for removing the pipeline of hydrogen-rich gas, for being pressurized to hydrogen-rich gas Booster compressor, for removing the pipeline of reforming reaction liquid product and for being pressurized to reforming reaction solution phase product Pump.Wherein, for catalytic reforming reaction product is fed be usually provided with the feeding line to the gas-liquid separator it is cold But device, for being cooled down to catalytic reforming reaction product.

Described reformation is again in contactor, for by the hydrogen-rich gas after supercharging and the production of the reforming reaction liquid phase after supercharging Thing is fed to cooler is generally also set up on the feeding line of contactor again, further to reduce the temperature of mixed feeding, is obtained More preferable lighter hydrocarbons recovery effect and the purity for improving hydrogen.

In the utility model, on the feeding line fed the mixed material from air and liquid mixer to hydrogenation reactor Heat riser can also be generally set, hydrogen and the again mixed feeding of contactor bottom of towe oil are heated to by heat riser The inlet temperature of hydrogen reactor.Or the hydrogen in any source can be being fed to gas-liquid with contactor bottom of towe oil is reformed again Heat riser is set on the feeding line of blender, after hydrogen and bottom of towe oil are preheated into reactor inlet temperature, then entered Enter air and liquid mixer and carry out molten hydrogen.

In the utility model, hydrogenation plant reaction product gas-liquid separator can be set, the gas phase and liquid phase after separation point Cut light tower is not introduced from suitable position.

In the utility model, the operation temperature of pre- hydrogenation plant is generally below 10~100 DEG C of hydrogenation plant.

Compared with prior art, the utility model has the advantages that：

1st, hydrogenation system of the present utility model can enter under the process conditions more relaxed to reforming reaction solution phase product Row depth-selectiveness is hydrogenated with, with remove carbon-carbon double bonds therein and/or or triple carbon-carbon bonds hydro carbons, aromatic hydrocarbons damages in hydrogenation process Vector can be controlled below 0.5 percentage point, therefore the reforming reaction liquid product after hydrogenation can meet downstream virtue completely Quality requirement of the hydrocarbon extraction device to charging.

2nd, because hydrogenation reactor is arranged on again between contactor and stabilizer, directly can be obtained using contactor again Appropriate amount of hydrogen is hydrogenated with the conditions of liquid-phase hydrogenatin, eliminates the circulating hydrogen compressor in existing hydrogenation system as hydrogen source, Reduce cost of investment and running cost.

3rd, because hydrogenation reactor is arranged on again between contactor and stabilizer, raw material heating and cooling process is reduced, thus The low level heat source of device can be taken full advantage of, reduces the operation energy consumption of device.

4th, reaction environment is mainly liquid phase reactor in hydrogenation reactor, has cut down the probability of bias current and channel appearance, has made dress It is more stable to put the reforming reaction liquid product property being refining to obtain.

5th, due in device separator hydrogen be unsaturated state, reduce enterprise's hydrogen loss or hydrogen recovery disappear Consumption, also reduces plant energy consumption.

6th, combined using pre- hydrogenation plant with hydrogenation plant, the low temperature active and high temperature of hydrogenation catalyst can be made full use of Activity, be advantageous to extend the service life of catalyst.

7th, by hydrogenation plant and the coupled relation of cut light tower, it ensure that hydrogenation plant in interior adjustment temperature in a big way When spending, the operation on cut light tower influences smaller.Hydrogenation plant reaction product is first cooled the heat exchange stream to be heated up afterwards Journey, although heating efficiency decreases in theory, it can ensure that the fluctuation of cut light tower inlet temperature is smaller.It is computed Show, when hydrogenation plant reaction temperature adjusts in the range of 100~230 DEG C, cut light tower inlet temperature fluctuation range is at 5 DEG C Left and right, and be macrocyclic slowly fluctuation, by the simple adjustment of cut light tower, its normal operating is not influenceed.During operation The operation of cut light tower is influenceed without worrying adjustment temperature of reactor.Under being discharged to outside the bottom of towe 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 the system and the operating of downstream processing unit automatic steady, are not required to excessive artificial regulation.

8th, the lighter hydrocarbons of reforming process reclaim in device, are not required to separately set light ends unit.

9th, it is big to boil system mass flow again for cut light tower, has power set, and the temperature for hydrogenation plant charging is adjusted It is whole that there is bigger adjustment space, higher adjustment flexibility, be advantageous to commercial plant stable operation.Cut light tower is boiled again System has a heating furnace, and the advantage of heating furnace is that regulation is sensitive, is influenceed by charging smaller, and therefore, above-mentioned adjustment does not influence to take off light group Divide the stable operation of tower.

10th, the system of boiling has heating furnace to cut light tower again, will be used for cut light tower by outer row's material of heating furnace The heat exchange of charging, because the temperature of the material is further lifted, can effective lifting system device stable operation elastic space, Hydrogenation reaction device can adjust in broader opereating specification, the stable operation without influenceing cut light tower.

Brief description of the drawings

Fig. 1, which is that the utility model is a kind of, forms schematic diagram.

Fig. 2, which is that the utility model is another, forms schematic diagram.

Embodiment

Reforming reaction liquid product hydrogenation system of the present utility model is carried out with specific embodiment below in conjunction with the accompanying drawings detailed Thin description.

As shown in figure 1, the utility model includes：Contactor 12 again are reformed, it includes the hydrogen-rich gas after by supercharging Charging is fed to the contactor again to the feeding line 9 of the contactor again and by the reforming reaction liquid product after supercharging Feeding line 8, for remove the hydrogen of hydrogen remove pipeline 13 and for remove again contactor generation oil removal pipeline 14.

Described reformation is again in contactor 12, for the hydrogen-rich gas after supercharging is fed into entering to the contactor again Cooler 11 is additionally provided with expects pipe line 9, the reforming reaction liquid product after supercharging is fed to the charging of the contactor again Cooler 10 can also be set on pipeline 8, further reduce the temperature of charging, returned with obtaining more preferable lighter hydrocarbons in contactor again Produce effects fruit and improve hydrogen purity.

Air and liquid mixer 15, it is included for will be fed from the bottom of towe oil for reforming again contactor to the air and liquid mixer Feeding line 14, for the hydrogen from any source is fed to the feeding line of the air and liquid mixer.Such as Fig. 1 institutes Show, in the present embodiment, for the hydrogen from any source to be fed to the feeding line of air and liquid mixer with reforming again The hydrogen removal pipeline 13 for being used for removing hydrogen in contactor is connected, i.e., the hydrogen in described any 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 mix with raw material.

Hydrogenation reactor 18, it is included for the mixed material from air and liquid mixer is fed to the hydrogenation reactor Feeding line 17, and for remove the hydrogenation products of hydrogenation products remove pipeline 19.

Hydrogenation reactor 18 generally includes more than two hydrogenation catalyst beds 24.Described hydrogenation system preferably also wraps Include with supplement hydrogen feeding line of the supplement from any source hydrogen between dealing two or more beds.In this embodiment party In formula, with the supplement hydrogen feeding line and reformation that the hydrogen from any source is supplemented between dealing two or more beds 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.

Described hydrogenation reactor 18 is liquid phase hydrogenation reactor（Predominantly liquid phase, small part are the gas of material gasification Phase）, it can be upper feeding or lower charging reactor, and lower charging reactor is preferably used in the utility model.

In described hydrogenation reactor 18, the mixed material from air and liquid mixer is being fed into entering to hydrogenation reactor Heat riser 16.3 is preferably provided with expects pipe line 17（Heat exchanger C）, for by hydrogen and again contactor bottom of towe oil mixed feeding The inlet temperature of hydrogenation reactor is heated to by heat riser.Or as needed can be by the hydrogen from contactor again Heat riser is set on gas and bottom of towe oil charging to 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 a portion of the outlet material of system delivery pump 31 again, i.e., the outlet line of delivery pump 31 heats with heat exchanger Stream inlet connects, and the outlet of heat exchanger heated stream connects with the entrance of reboiler furnace 32, 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 Adjusting means, to adjust the logistics flux into heat exchanger.

In the utility model, in addition to gas-liquid separator 3, it includes being fed catalytic reforming reaction product to institute with dealing The feeding line 1 of gas-liquid separator 3 is stated, for removing the pipeline 4 of hydrogen-rich gas, the supercharging for being pressurized to hydrogen-rich gas Compressor 5, for removing the pipeline 6 of reforming reaction liquid product and for reforming the pump 7 that is pressurized of reaction solution phase product. Wherein, it is being additionally provided with cooler on the feeding line 1 to the gas-liquid separator 3 for catalytic reforming reaction product is fed 2, for being cooled down to catalytic reforming reaction product.

In the utility model, cut light tower 20（Also referred to as stabilizer）, it is included for liquid phase hydrogenation reactor is hydrogenated with Product is fed to the feeding line 19 of the cut light tower, the feeding line is used as the hydrogenation products of hydrogenation reactor 18 simultaneously Pipeline is removed, pipeline 21 is removed and for by reforming reaction liquid for removing the overhead product of cut light tower overhead gas product The removal pipeline 22 that phase product is discharged from cut light tower.

The outlet of reboiler furnace 32 of cut light tower sets gas-liquid separator 33, and the gaseous phase outlet of gas-liquid separator 33 passes through pipeline Connected with cut light tower, gas-liquid separator liquid-phase outlet passes through the heat exchanger that is set on pipeline and cut light tower feeding line 16.2 connections, realize that the cut light tower discharge material after heating adjusts to the heat-exchange temperature for taking off light component charging.

In the utility model, hydrogenation reactor discharges first in heat exchanger 16.1（Heat exchanger A）In enter with hydrogenation reactor Material heat exchange（Cooling）Afterwards, then in heat exchanger 16.2（Heat exchanger B）In with cut light tower bottom of towe discharge exchange heat（Heating）, Ran Houjin Enter cut light tower and carry out fractionation processing.Hydrogenation reactor discharging by first cool afterwards heat up adjustment, meet take off gently well The stable requirement of component tower feeding temperature.If without the adjustment of cooling, heating heat exchange, cut light tower charging are directly carried out Temperature can improve with the raising of hydrogenation reactor temperature, the final normal operating for influenceing cut light tower.

Fig. 2 show the composition schematic diagram of the utility model another kind embodiment.Wherein chief component is same Flow in Fig. 1, is repeated no more.

Wherein difference part is, pre-hydrogenator 23 is set before hydrogenation reactor, and pre-hydrogenator 23 enters 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 Exchanged heat by heat exchanger 16.2（Cooling）Cut light tower bottom of towe discharge material etc..

With reference to Fig. 1, a kind of technical process that the utility model is used for reforming reaction liquid product hydrogenation is：

Reforming reaction product from reforming reactor is separated after pipeline 1, cooler 2 into gas-liquid separator 3, Pass through isolated hydrogen-rich gas and reforming reaction liquid product wherein.The gained hydrogen-rich gas of gas-liquid separator 3 enters through pipeline 4 Enter booster compressor 5 to be pressurized, gained reforming reaction liquid product is pressurized through pipeline 6 into pump 7.Hydrogen-rich after supercharging For gas through pipeline 9 and cooler 11, the reforming reaction liquid product after supercharging respectively enters weight after pipeline 8 and cooler 10 Whole contactor 12 again, further remove the lighter hydrocarbons contained in hydrogen-rich gas.Reform again contactor 12 and obtain the hydrogen warp of high-purity Hydrogen remove pipeline 13 remove, all the way through pipeline with by the reformation of pipeline 14 again contactor bottom of towe oil mix after through heating, Air and liquid mixer 15 and pipeline 17, or enter hydrogenation reactor 18 through pipeline 17 after air and liquid mixer 15 and heating, with Hydrogenation catalyst contact containing active component platinum carries out liquid-phase hydrogenatin reaction, removes in reforming reaction liquid product and contains carbon carbon The hydrocarbon impurities of double bond and/or triple carbon-carbon bonds；The another way for reforming again the high-purity hydrogen that contactor obtains is followed through pipeline entrance Ring hydrogen compressor or separating device, the 3rd road hydrogen can be set to enter the two or more of hydrogenation reactor 18 by pipeline and be hydrogenated with Between beds 24, as supplement hydrogen.The hydrogenated product of hydrogenation reaction product removes pipeline 19 and first passes through heat exchanger 16.1 Cooling, then heat exchanger 16.2 enters stabilizer 20 after after heating up, obtained gaseous product removes pipeline 21 by overhead product Discharge, the reforming reaction liquid product for obtaining impurity content reduction are discharged through pipeline 22.

Claims (12)

1. a kind of recapitalization generating oil hydrogenation device and cut light tower coupled system, including：

Hydrogenation plant, it includes the feeding line for hydrogenation plant charging to be led to the hydrogenation reaction device, and for moving The hydrogenation products for going out hydrogenation products remove pipeline；

Cut light tower, it includes the feeding line that the cut light tower is led to for cut light tower is fed, and is 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 towe heavy constituent obtained after fractionation Pipeline；Also include boiling system again, specifically include delivery pump, reboiler furnace and supporting pipelines and control system；

Hydrogenation plant includes with cut light tower coupled relation：Reboiler furnace outlet sets gas-liquid separator, gas-liquid separator gas phase Outlet is boiled material inlet with cut light tower by pipeline and connected again, and gas-liquid separator liquid-phase outlet passes through pipeline and de- light component The heat exchanger B connections set on tower feeding line.

2. system according to claim 1, it is characterised in that：Hydrogenation plant includes with cut light tower coupled relation：Add Heat riser and temperature control equipment are set on hydrogen production device feeding line, for regulating and controlling hydrogenation plant reaction temperature, heat riser For heat exchanger C, exchanger heat logistics is to boil at least a portion of system delivery pump outlet material again, i.e., delivery pump outlet line with Heat exchanger C heated streams entrance connects, and the outlet of heat exchanger C heated streams connects with reboiler furnace entrance, and reboiler furnace outlet is light with taking off Component tower boils material inlet connection again.

3. system according to claim 1, it is characterised in that：Heat exchanger A cold material feeds for hydrogenation plant, heat exchanger B thermal material is the bottom of towe heavy constituent of cut light tower.

4. system according to claim 1, it is characterised in that：Pre- hydrogenation plant is set before hydrogenation plant, than hydrogenation Operated at the low temperature of device, pre- hydrogenation plant outlet line connects with heat exchanger A.

5. system according to claim 4, it is characterised in that：Hydrogenation plant and/or pre- hydrogenation plant set hydrogen make Pipeline and hydrogen amount control device.

6. system according to claim 5, 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.

7. system according to claim 4, 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 aluminum oxide.

8. system according to claim 6, it is characterised in that：Air and liquid mixer is static mixer or dynamic mixer.

9. 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.

10. system according to claim 4, it is characterised in that：The operation temperature of pre- hydrogenation plant is less than hydrogenation plant 10 ~100 DEG C.

11. system according to claim 2, it is characterised in that：Set between heat exchanger C heated streams entrance and outlet Cross-line, flow regulator is set on cross-line, to adjust the logistics flux into heat exchanger C.

12. system according to claim 1, it is characterised in that：Hydrogenation plant includes with cut light tower coupled relation：Its The heat exchanger A and heat exchanger B that are set on pipeline are removed including hydrogenation products, hydrogenation products remove pipeline and connected with heat exchanger A, then Connected through pipeline with heat exchanger B, hydrogenation products remove pipeline, and most the feeding line through cut light tower connects with cut light tower afterwards It is logical；Heat exchanger B thermal material is boils the liquid phase material that system furnace outlet gas-liquid separator obtains again, i.e. cut light tower Outer row's bottom of towe heavy constituent.