CN107619680A - A kind of system and technique of diesel hydrotreating unit naphtha direct-furnish reformer - Google Patents
A kind of system and technique of diesel hydrotreating unit naphtha direct-furnish reformer Download PDFInfo
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- CN107619680A CN107619680A CN201710964249.8A CN201710964249A CN107619680A CN 107619680 A CN107619680 A CN 107619680A CN 201710964249 A CN201710964249 A CN 201710964249A CN 107619680 A CN107619680 A CN 107619680A
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Abstract
The invention discloses a kind of system and technique of diesel hydrotreating unit naphtha direct-furnish reformer, using raw material direct-furnish technique, its technological process is：Diesel hydrotreating unit mixed feeding, into fractionating system stripper and fractionating column, sends pump outside by naphtha and naphtha is fed directly into the pre- hydrogenation unit stripper entrance of reformer after heating furnace, hydrofining reactor, hydro-upgrading reactor for treatment.The present invention use the pre- hydrogenation unit stripper of diesel hydrotreating unit naphtha direct-furnish reformer, make it compared with prior art, have technological process shortening, energy consumption is small, it is easy to operate the advantages of.
Description
Technical field
The present invention relates to petrochemical industry, specifically a kind of system of diesel hydrotreating unit naphtha direct-furnish reformer
And technique.
Background technology
At present, diesel hydrotreating unit naphtha（Distillate hydrogenation naphtha）It is typically outer to deliver to when delivering to reformer outside
Reformer is hydrogenated with unit naphtha tank in advance, with remaining species naphtha（Such as atmospheric and vacuum distillation unit come straight-run naphtha, from burnt
Change the coking naphtha of gasoline and diesel hydrogenation）Carried out hydrofinishing, stripping again together, it is qualified so as to be provided to reformer unit
Raw material；The technological process is longer, and energy consumption is preferable.But diesel hydrotreating unit naphtha quality standard is higher, and from Atmospheric vacuum
The straight-run naphtha of device, the coking naphtha quality from coking gasoline and diesel hydrogenation are relatively low, after three kinds of naphthas mixing, need
To pass through the flow such as heat exchange process and pre- hydrogenation charging heating furnace, pre-hydrogenator to be handled；Add the diesel oil of high-quality
Hydrogen production device naphtha has walked a hydrotreating flow again, so that energy consumption increases, the increase of operating procedure difficulty, potential safety hazard
Increase.
The content of the invention
The defects of purpose of the present invention exists aiming at prior art, there is provided a kind of technique is simple and convenient to operate and energy
Consume the system and technique of small diesel hydrotreating unit naphtha direct-furnish reformer.
A kind of system of diesel hydrotreating unit naphtha direct-furnish reformer is provided first, including the diesel oil of interconnection adds
Hydrogen production device and reformer stripper, the diesel hydrotreating unit include passing sequentially through heating furnace, the hydrofinishing of pipeline connection
Reactor, hydro-upgrading reactor, high pressure hot separator, thermal low-pressure separators, cold low separator and fractionating system, it is described
Heating furnace entrance connects diesel feed pipeline；The fractionating system includes the stripper and fractionating column being sequentially connected, the stripping
The top of tower is provided with return tank, and connects and composes stripper overhead return-flow system by reflux pipeline；The fractionator overhead is set
There is naphtha discharging pipeline, the naphtha discharging pipeline is provided with Liang Ge branches, wherein a connection return tank, and pass through backflow
Pipeline connects and composes fractionator overhead return-flow system, and another is directly connected with reformer stripper entrance.
Further, described diesel hydrotreating unit also includes heat exchanger, the cold medium flow and diesel oil of the heat exchanger
Feeding line connects, and the cold medium flow of the heat exchanger is connected to the pipe between hydro-upgrading reactor, high pressure hot separator
On line；Filter is also associated with the diesel feed pipeline of the heat exchanger front end.
Further, the diesel hydrotreating unit also includes cold high pressure separator；The bottom of the high pressure hot separator goes out
Mouth connects thermal low-pressure separators inlet line by pipeline, top exit passes through the inlet tube that pipeline connects cold high pressure separator
Line；The inlet line of the top exit connection cold low separator of the thermal low-pressure separators；The bottom of the thermal low-pressure separators
Portion is exported and the outlet at bottom of cold low separator is connected by pipeline and after connecing with fractionating system；The cold high pressure separator
Outlet at bottom is attempted by by pipeline in the inlet line of cold low separator；The top exit of the cold high pressure separator passes through
Pipeline connects the import of desulphurization of recycle hydrogen tower, and the outlet of the desulphurization of recycle hydrogen tower connects entering for circulating hydrogen compressor by pipeline
Mouthful, the outlet line of the circulating hydrogen compressor is provided with branch and entered respectively with hydrofining reactor, hydro-upgrading reactor
Hydrogen pipeline connects.
Further, the system also includes the pre- hydrogenation unit of reformer, and the pre- hydrogenation unit of reformer includes
The mixing naphtha tank that is sequentially connected by pipeline, pre- hydrogenation feed surge tank, charge filter, heating furnace, pre-add are hydrogenated with advance
Hydrogen reactor, pre-add dechlorination reaction device, pre- hydrogenation products air cooler and pre- hydrogenation liquid/gas separator；The mixing naphtha tank
Entrance connects the straight-run naphtha feeding line come from atmospheric and vacuum distillation unit and the coking stone brain come from coking gasoline and diesel hydrogenation respectively
Oily feeding line；Pre- hydrogenation mixed feeding heat exchanger is also associated between the pre- hydrogenation charge filter, heating furnace, it is described pre-
The disengaging both ends for being hydrogenated with the cold medium flow of mixed feeding heat exchanger pass through pipeline with pre- hydrogenation charge filter, heating furnace respectively
Connection, it is described it is pre- hydrogenation mixed feeding heat exchanger thermal medium flow disengaging both ends respectively with pre-add dechlorination reaction device, pre-add
Hydrogen product air cooler is connected by pipeline；The upper outlet pipeline connection circulating hydrogen compressor of the pre- hydrogenation liquid/gas separator enters
Mouth liquid separation tank, the upper outlet pipeline of the circulating hydrogen compressor entrance liquid separation tank are attempted by by being hydrogenated with circulating hydrogen compressor in advance
On pipeline between pre- hydrogenation charge filter and pre- hydrogenation mixed feeding heat exchanger, the circulating hydrogen compressor entrance liquid separation tank
Lower part outlet pipeline be attempted by the lower part outlet pipeline of pre- hydrogenation liquid/gas separator, under the pre- hydrogenation liquid/gas separator
Portion's outlet line is connected with reformer stripper；The company of the pre- hydrogenation mixed feeding heat exchanger and pre- hydrogenation products air cooler
On adapter line and supplement hydrogen pipeline is connected to, the supplement hydrogen pipeline is connected with supplement hydrogen compressor entrance liquid separation in turn from front to back
Tank, pre- hydrogenation supplement hydrogen compressor, the entrance point and pre- hydrogenation of the supplement hydrogen compressor entrance liquid separation tank supplement hydrogen compressor
The port of export and be connected to supplement hydrogen recirculation cooler.
Further, the naphtha discharging pipeline of the diesel hydrotreating unit is provided with branch and is connected with mixing naphtha tank.
Then a kind of technique of the diesel hydrotreating unit naphtha direct-furnish reformer using said system, its technique are provided
Flow is after diesel hydrotreating unit mixed feeding first passes around heating furnace heating, then hydrogenated finishing reactor, hydrogenation successively
After reforming reactor carries out hydrotreating, the stripper of fractionating system is then entered after each separator carries out Oil-gas Separation and is divided
Tower is evaporated, fractionating column sends produced naphtha outside pump by naphtha and is fed directly to reformer stripper.
Further, the hydro-upgrading reactor inlet temperature controls 320-330 DEG C, hydrogen-oil ratio control 600-700, sky
Speed control 0.85-0.95 h-2。
Further, the stripper steam injection amount control 2.5-3.2t/h of the fractionating system.
Further, the sulfur content control of the fractionating column direct-furnish reformer stripper naphtha is less than 0.5ppm.
Further, the next straight-run naphtha of described atmospheric and vacuum distillation unit and the coking stone brain come from coking gasoline and diesel hydrogenation
After oil first passes around the pre- hydrogenation unit progress hydrotreating of reformer, subsequently into reformer stripper.
The technique of the present invention is using diesel hydrotreating unit naphtha without the pre- hydrogenation unit direct-furnish of existing reformer
The pre- hydrogenation unit stripper of reformer, makes it compared with prior art, there is technological process to shorten, energy consumption is small, operation side
Just the advantages of；Simultaneously can be different according to the quality of naphtha and source, flexibly using different handling process, expand whole
The application of set system and technique.
Brief description of the drawings
Fig. 1 is a kind of flow chart of diesel hydrotreating unit naphtha direct-furnish reformer technique；
The process chart that a kind of naphtha reformings of Fig. 2 are hydrogenated with advance；
In figure：1st, heat exchanger, 2, heating furnace, 3, hydrofining reactor, 4, hydro-upgrading reactor, 5, high pressure hot separator,
6th, thermal low-pressure separators, 7, cold low separator, 8, cold high pressure separator, 9, stripper, 10, stripping return tank of top of the tower, 11, point
Evaporate tower, 12, fractionation return tank of top of the tower, 13, desulphurization of recycle hydrogen tower, 14, circulating hydrogen compressor；101st, feed surge tank is hydrogenated with advance,
102nd, it is hydrogenated with feed pump in advance, 103, be hydrogenated with charge filter in advance, 104, pre- hydrogenation mixed feeding heat exchanger, 105, pre- hydrogenation charging
Heating furnace, 106, pre-hydrogenator, 107, pre-add dechlorination reaction device, 108, pre- hydrogenation liquid/gas separator, 109, recycle hydrogen pressure
Contracting machine entrance liquid separation tank, 110, be hydrogenated with circulating hydrogen compressor in advance, 111, supplement hydrogen compressor entrance liquid separation tank, 112, pre- hydrogenation mends
It is flushed with hydrogen compressor, 113, supplement hydrogen recirculation cooler, 114, pre- hydrogenation products air cooler.
Embodiment
Below in conjunction with specific embodiments and the drawings, the present invention is described further.
Embodiment 1
Referring to Fig. 1, a kind of system of diesel hydrotreating unit naphtha direct-furnish reformer, the diesel oil hydrogenation for including interconnection fills
Put includes the heat exchanger 1, heating furnace 2, hydrofinishing for passing sequentially through pipeline connection with reformer stripper, diesel hydrotreating unit
Reactor 3, hydro-upgrading reactor 4, high pressure hot separator 5, thermal low-pressure separators 6, cold low separator 7, cold anticyclone separation
Device 8 and fractionating system, the entrance of heating furnace 2 connection diesel feed pipeline；Fractionating system includes the stripper 9 being sequentially connected and divided
Tower 11 is evaporated, the top of stripper 9 is provided with stripping return tank of top of the tower 10, and connects and composes stripper overhead by reflux pipeline and flow back
System；The tower top of fractionating column 11 is provided with naphtha discharging pipeline, and naphtha discharging pipeline is provided with Liang Ge branches, wherein a connection point
Evaporate return tank of top of the tower 12, and fractionator overhead return-flow system is connected and composed by reflux pipeline, another directly and reformer
Stripper entrance connects.
The cold medium flow of heat exchanger 1 is connected with diesel feed pipeline, and the cold medium flow of heat exchanger 1 is connected to hydrogenation and changed
On pipeline between qualitative response device 4, high pressure hot separator 5；It is also associated with filtering on the diesel feed pipeline of the front end of heat exchanger 1
Device.
The outlet at bottom of high pressure hot separator 5 connects the inlet line of thermal low-pressure separators 6 by pipeline, top exit leads to
Cross the inlet line of pipeline connection cold high pressure separator 8；The top exit connection cold low separator 7 of thermal low-pressure separators 6
Inlet line；The outlet at bottom of thermal low-pressure separators 6 and the outlet at bottom of the separator of cold low 7 by pipeline and connect rear with being fractionated
System is that stripper 9 connects；The outlet at bottom of cold high pressure separator 8 is attempted by the inlet tube of cold low separator 7 by pipeline
On line；The top exit of cold high pressure separator 8 connects the import of desulphurization of recycle hydrogen tower 13 by pipeline, desulphurization of recycle hydrogen tower 13
Outlet connects the import of circulating hydrogen compressor 14 by pipeline, and the outlet line of circulating hydrogen compressor 14 is provided with branch respectively with adding
Hydrogen finishing reactor 3, the hydrogen pipeline of entering of hydro-upgrading reactor 4 connect.
Technological process is：After diesel hydrotreating unit mixed feeding first passes around filter filtering, then through heat exchanger 1 with adding
After the heat exchange of hydrogen product, heated up into heating furnace 2, then hydrogenated finishing reactor 3, hydro-upgrading reactor 4 are added successively
After hydrogen processing, then hydrogenation products enter the stripper 9 and fractionating column 10 of fractionating system after each separator carries out Oil-gas Separation,
Fractionating column 10 sends produced naphtha outside pump by naphtha and is fed directly to reformer stripper.Technology controlling and process：Modification reaction
Device inlet temperature controls 320-330 DEG C, hydrogen-oil ratio control 600-700, air speed control 0.85-0.95 h-2；Fractionating system stripper
Steam injection amount controls 2.5-3.2t/h；The control of direct-furnish naphtha sulfur content is less than 0.5ppm.
Embodiment 2
In order to meet that the reformation of the naphtha of different qualities and source is handled, on the basis of embodiment 1, the system also includes
The pre- hydrogenation unit of reformer, referring to Fig. 2, the pre- hydrogenation unit of reformer includes the mixing naphtha being sequentially connected by pipeline
Tank, pre- hydrogenation feed surge tank 101, pre- hydrogenation feed pump 102, pre- hydrogenation charge filter 103, pre- hydrogenation mixed feeding heat exchange
Device 104, pre- hydrogenation charging heating furnace 105, pre-hydrogenator 106, pre-add dechlorination reaction device 107, pre- hydrogenation products air cooler
114 and pre- hydrogenation liquid/gas separator 108；Mixing naphtha tank entrance connects the straight-run naphtha come from atmospheric and vacuum distillation unit respectively
Feeding line and the coking naphtha feeding line come from coking gasoline and diesel hydrogenation, the naphtha discharging pipeline of diesel hydrotreating unit
（That is the distillate hydrogenation naphtha in Fig. 2 carrys out shown pipeline from diesel oil hydrogenation modification）Branch is provided with mixing naphtha tank
Connection；The disengaging both ends of the cold medium flow of pre- hydrogenation mixed feeding heat exchanger 104 respectively with pre- hydrogenation charge filter 103,
Pre- hydrogenation charging heating furnace 105 is connected by pipeline, the disengaging both ends of the pre- thermal medium flow for being hydrogenated with mixed feeding heat exchanger 104
It is connected respectively with pre-add dechlorination reaction device 107, pre- hydrogenation products air cooler 114 by pipeline；Pre- hydrogenation liquid/gas separator 108
Upper outlet pipeline connection circulating hydrogen compressor entrance liquid separation tank 109, the upper outlet of circulating hydrogen compressor entrance liquid separation tank 109
Pipeline is attempted by pre- hydrogenation charge filter 103 and pre- hydrogenation mixed feeding heat exchanger by being hydrogenated with circulating hydrogen compressor 110 in advance
On pipeline between 104, the lower part outlet pipeline of circulating hydrogen compressor entrance liquid separation tank 109 is attempted by pre- hydrogenation liquid/gas separator
On 108 lower part outlet pipeline, the lower part outlet pipeline of pre- hydrogenation liquid/gas separator 108 is connected with reformer stripper；In advance
In the connecting pipeline of hydrogenation mixed feeding heat exchanger 104 and pre- hydrogenation products air cooler 114 and supplement hydrogen pipeline is connected to, supplements hydrogen
Pipeline is connected with supplement hydrogen compressor entrance liquid separation tank 111, pre- hydrogenation supplement hydrogen compressor 112 in turn from front to back, supplements hydrogen
The entrance point of suction port of compressor liquid separation tank 111 and pre- hydrogenation supplement the port of export of hydrogen compressor 112 and to be connected to supplement hydrogen circulation cold
But device 113.
Technological process is：Diesel hydrotreating unit naphtha can do two kinds of selections according to the difference of quality, when quality is higher
When be directly entered reformer stripper, when quality is relatively low, and atmospheric and vacuum distillation unit come straight-run naphtha, from coking gasoline and diesel
After the coking naphtha that hydrogenation comes first passes around the pre- hydrogenation unit progress hydrotreating of reformer together, filled subsequently into reforming
Put stripper.
Compared to existing design, i.e. hydro-upgrading unit naphtha direct-furnish to reformer is hydrogenated with unit naphtha tank in advance, with
Remaining naphtha carries out hydrofinishing, stripping together, there is provided the qualified raw material of reformer unit；The diesel oil hydrogenation modification warp of the present invention
Cross optimization and produce qualified reformer feed, this part naphtha is directly entered stripper, can reduce weight without hydrofinishing
Whole pretreatment unit raw material pump load 22%, heating furnace load 25% is reduced, reduce catalyst space velocities 25%.Reformed pre-hydrogenated unit
Energy-conservation 15% or so.
As it will be easily appreciated by one skilled in the art that the foregoing is merely illustrative of the preferred embodiments of the present invention, not to
The limitation present invention, all any modification, equivalent and improvement made within the spirit and principles of the invention etc., all should be included
Within protection scope of the present invention.
Claims (10)
- A kind of 1. system of diesel hydrotreating unit naphtha direct-furnish reformer, it is characterised in that：Diesel oil including interconnection Hydrogenation plant and reformer stripper, the diesel hydrotreating unit include passing sequentially through the heating furnace of pipeline connection, hydrogenation essence Reactor, hydro-upgrading reactor, high pressure hot separator, thermal low-pressure separators, cold low separator and fractionating system processed, institute State heating furnace entrance connection diesel feed pipeline；The fractionating system includes the stripper and fractionating column being sequentially connected, the vapour The top of stripper is provided with return tank, and connects and composes stripper overhead return-flow system by reflux pipeline；The fractionator overhead Provided with naphtha discharging pipeline, the naphtha discharging pipeline is provided with Liang Ge branches, wherein a connection return tank, and by returning Flow tube line connects and composes fractionator overhead return-flow system, and another is directly connected with reformer stripper entrance.
- 2. the system of diesel hydrotreating unit naphtha direct-furnish reformer according to claim 1, it is characterised in that：It is described Diesel hydrotreating unit also include heat exchanger, the cold medium flow of the heat exchanger is connected with diesel feed pipeline, the heat exchange The cold medium flow of device is connected on the pipeline between hydro-upgrading reactor, high pressure hot separator；The heat exchanger front end Filter is also associated with diesel feed pipeline.
- 3. the system of diesel hydrotreating unit naphtha direct-furnish reformer according to claim 1, it is characterised in that：It is described Diesel hydrotreating unit also includes cold high pressure separator；The outlet at bottom of the high pressure hot separator connects heat low point by pipeline The inlet line of cold high pressure separator is connected by pipeline from device inlet line, top exit；The top of the thermal low-pressure separators The inlet line of portion outlet connection cold low separator；The outlet at bottom of the thermal low-pressure separators and the bottom of cold low separator Portion outlet is connected by pipeline and after connecing with fractionating system；The outlet at bottom of the cold high pressure separator is attempted by cold by pipeline In the inlet line of low pressure separator；The top exit of the cold high pressure separator connects entering for desulphurization of recycle hydrogen tower by pipeline Mouthful, the outlet of the desulphurization of recycle hydrogen tower connects the import of circulating hydrogen compressor by pipeline, and the circulating hydrogen compressor goes out Mouth pipeline is connected provided with hydrogen pipeline of entering of the branch respectively with hydrofining reactor, hydro-upgrading reactor.
- 4. the system of diesel hydrotreating unit naphtha direct-furnish reformer according to claim 1, it is characterised in that：It is described System also includes the pre- hydrogenation unit of reformer, and the pre- hydrogenation unit of reformer includes the mixing being sequentially connected by pipeline Naphtha tank, pre- hydrogenation feed surge tank, charge filter, heating furnace, pre-hydrogenator, pre-add dechlorination reaction are hydrogenated with advance Device, pre- hydrogenation products air cooler and pre- hydrogenation liquid/gas separator；The mixing naphtha tank entrance connects from Atmospheric vacuum respectively The next straight-run naphtha feeding line of device and the coking naphtha feeding line come from coking gasoline and diesel hydrogenation；The pre- hydrogenation Pre- hydrogenation mixed feeding heat exchanger is also associated between charge filter, heating furnace, the pre- hydrogenation mixed feeding heat exchanger The disengaging both ends of cold medium flow are connected with pre- hydrogenation charge filter, heating furnace by pipeline respectively, the pre- hydrogenation mixing The disengaging both ends of the thermal medium flow of feed exchanger pass through pipeline with pre-add dechlorination reaction device, pre- hydrogenation products air cooler respectively Connection；The upper outlet pipeline connection circulating hydrogen compressor entrance liquid separation tank of the pre- hydrogenation liquid/gas separator, the recycle hydrogen The upper outlet pipeline of suction port of compressor liquid separation tank by be hydrogenated with advance circulating hydrogen compressor be attempted by it is pre- hydrogenation charge filter and On pipeline between pre- hydrogenation mixed feeding heat exchanger, the lower part outlet pipeline of the circulating hydrogen compressor entrance liquid separation tank simultaneously connects On the lower part outlet pipeline of pre- hydrogenation liquid/gas separator, the lower part outlet pipeline of the pre- hydrogenation liquid/gas separator fills with reforming Put stripper connection；In the connecting pipeline of pre- hydrogenation mixed feeding heat exchanger and the pre- hydrogenation products air cooler and it is connected to supplement Hydrogen pipeline, the supplement hydrogen pipeline are connected with supplement hydrogen compressor entrance liquid separation tank, pre- hydrogenation supplement hydrogen pressure in turn from front to back Contracting machine, the entrance point and pre- hydrogenation of the supplement hydrogen compressor entrance liquid separation tank supplement the port of export of hydrogen compressor and are connected to supplement Hydrogen recirculation cooler.
- 5. the system of diesel hydrotreating unit naphtha direct-furnish reformer according to claim 4, it is characterised in that：It is described The naphtha discharging pipeline of diesel hydrotreating unit is provided with branch and is connected with mixing naphtha tank.
- 6. a kind of technique of diesel hydrotreating unit naphtha direct-furnish reformer using any systems of claim 1-5, It is characterized in that：Its technological process is after diesel hydrotreating unit mixed feeding first passes around heating furnace heating, then successively through adding After hydrogen finishing reactor, hydro-upgrading reactor carry out hydrotreating, then enter after each separator carries out Oil-gas Separation and divide The stripper and fractionating column of system are evaporated, fractionating column sends produced naphtha outside pump by naphtha and is fed directly to reformer stripping Tower.
- 7. the technique of diesel hydrotreating unit naphtha direct-furnish reformer according to claim 6, it is characterised in that：It is described Hydro-upgrading reactor inlet temperature controls 320-330 DEG C, hydrogen-oil ratio control 600-700, air speed control 0.85-0.95 h-2。
- 8. diesel hydrotreating unit naphtha direct-furnish reformer technique according to claim 6, it is characterised in that：Described point Evaporate the stripper steam injection amount control 2.5-3.2t/h of system.
- 9. diesel hydrotreating unit naphtha direct-furnish reformer technique according to claim 6, it is characterised in that：Described point The sulfur content control for evaporating tower direct-furnish reformer stripper naphtha is less than 0.5ppm.
- 10. according to any described diesel hydrotreating unit naphtha direct-furnish reformer techniques of claim 6-9, its feature exists In：The straight-run naphtha and first pass around reformation from the next coking naphtha of coking gasoline and diesel hydrogenation that described atmospheric and vacuum distillation unit comes After the pre- hydrogenation unit of device carries out hydrotreating, subsequently into reformer stripper.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201710964249.8A CN107619680B (en) | 2017-10-17 | 2017-10-17 | System and process for naphtha direct-supply reforming device of diesel hydrogenation device |
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| CN201710964249.8A CN107619680B (en) | 2017-10-17 | 2017-10-17 | System and process for naphtha direct-supply reforming device of diesel hydrogenation device |
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| CN113943588A (en) * | 2020-07-16 | 2022-01-18 | 中国石油化工股份有限公司 | Naphtha fractionation process after pre-hydrogenation treatment of continuous reforming device |
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| Publication number | Publication date |
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| CN107619680B (en) | 2023-08-08 |
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