CN107619680B - System and process for naphtha direct-supply reforming device of diesel hydrogenation device - Google Patents
System and process for naphtha direct-supply reforming device of diesel hydrogenation device Download PDFInfo
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- CN107619680B CN107619680B CN201710964249.8A CN201710964249A CN107619680B CN 107619680 B CN107619680 B CN 107619680B CN 201710964249 A CN201710964249 A CN 201710964249A CN 107619680 B CN107619680 B CN 107619680B
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Abstract
The invention discloses a system and a process for a naphtha direct-supply reforming device of a diesel hydrogenation device, which adopts a raw material direct-supply process, and comprises the following process flows: the mixed feed of the diesel hydrogenation device is treated by a heating furnace, a hydrofining reactor and a hydro-upgrading reactor, then enters a fractionating system stripping tower and a fractionating tower, and naphtha is directly sent to the inlet of a reforming device pre-hydrogenation unit stripping tower through a naphtha external pump. Compared with the prior art, the method has the advantages of shortening the process flow, reducing the energy consumption and being convenient to operate by adopting the diesel hydrogenation device naphtha direct-supply reforming device prehydrogenation unit stripping tower.
Description
Technical Field
The invention relates to the field of petrochemical industry, in particular to a system and a process of a naphtha direct-supply reforming device of a diesel hydrogenation device.
Background
At present, when naphtha (distillate hydrogenated naphtha) of a diesel hydrogenation device is sent to a reforming device, the naphtha is generally sent to a naphtha tank of a pre-hydrogenation unit of the reforming device, and is subjected to hydrofining and steam stripping together with other naphtha types (such as straight-run naphtha from an atmospheric and vacuum device and coker naphtha from the hydrogenation of coker gasoline and diesel), so as to provide qualified raw materials for the reforming unit; the process flow is longer and the energy consumption is better. However, the naphtha quality standard of the diesel hydrogenation device is higher, the quality of straight-run naphtha from the atmospheric and vacuum device and the quality of coker naphtha from the hydrogenation of coker gasoline and diesel are lower, and after the three naphthas are mixed, the treatment is carried out through a heat exchange flow, a pre-hydrogenation feeding heating furnace, a pre-hydrogenation reactor and other flows; the naphtha of the high-quality diesel hydrogenation device is led to walk through the hydrotreating process again, so that the energy consumption is increased, the operation process difficulty is increased, and the potential safety hazard is increased.
Disclosure of Invention
The invention aims at overcoming the defects of the prior art and provides a system and a process for directly supplying naphtha to a reforming device of a diesel hydrogenation device, wherein the system is simple in process, convenient to operate and low in energy consumption.
Firstly, a system for directly supplying naphtha to a reforming device of a diesel hydrogenation device is provided, the system comprises the diesel hydrogenation device and a reforming device stripping tower which are connected with each other, the diesel hydrogenation device comprises a heating furnace, a hydrofining reactor, a hydro-upgrading reactor, a hot high-pressure separator, a hot low-pressure separator, a cold low-pressure separator and a fractionation system which are connected with each other through pipelines in sequence, and an inlet of the heating furnace is connected with a diesel feeding pipeline; the fractionating system comprises a stripping tower and a fractionating tower which are sequentially connected, wherein the top of the stripping tower is provided with a reflux tank and is connected with the reflux tank through a reflux pipeline to form a top reflux system of the stripping tower; the top of the fractionating tower is provided with a naphtha discharging pipeline, the naphtha discharging pipeline is provided with two branches, one branch is connected with a reflux tank and is connected with a reflux system at the top of the fractionating tower through the reflux pipeline, and the other branch is directly connected with the inlet of the stripping tower of the reforming device.
Further, the diesel hydrogenation device also comprises a heat exchanger, wherein the cold medium flow of the heat exchanger is connected with a diesel feeding pipeline, and the cold medium flow of the heat exchanger is connected to a pipeline between the hydro-upgrading reactor and the hot high-pressure separator; and a filter is also connected to the diesel oil feeding pipe at the front end of the heat exchanger.
Further, the diesel hydrogenation device also comprises a cold high-pressure separator; the bottom outlet of the hot high-pressure separator is connected with the inlet pipeline of the hot low-pressure separator through a pipeline, and the top outlet of the hot high-pressure separator is connected with the inlet pipeline of the cold high-pressure separator through a pipeline; the top outlet of the hot low-pressure separator is connected with the inlet pipeline of the cold low-pressure separator; the bottom outlet of the hot low-pressure separator and the bottom outlet of the cold low-pressure separator are connected in parallel through pipelines and then connected with a fractionation system; the bottom outlet of the cold high-pressure separator is connected in parallel with the inlet pipeline of the cold low-pressure separator through a pipeline; the top outlet of the cold high-pressure separator is connected with the inlet of the circulating hydrogen desulfurization tower through a pipeline, the outlet of the circulating hydrogen desulfurization tower is connected with the inlet of the circulating hydrogen compressor through a pipeline, and the outlet pipeline of the circulating hydrogen compressor is provided with branches which are respectively connected with the hydrogen inlet pipelines of the hydrofining reactor and the hydro-upgrading reactor.
Further, the system also comprises a reforming device pre-hydrogenation unit, wherein the reforming device pre-hydrogenation unit comprises a mixed naphtha tank, a pre-hydrogenation feed buffer tank, a pre-hydrogenation feed filter, a heating furnace, a pre-hydrogenation reactor, a pre-addition dechlorination reactor, a pre-hydrogenation product air cooler and a pre-hydrogenation gas-liquid separator which are connected in sequence through pipelines; the inlet of the mixed naphtha tank is respectively connected with a straight-run naphtha feeding pipeline from the atmospheric and vacuum device and a coker naphtha feeding pipeline from the hydrogenation of coker gasoline and diesel; a pre-hydrogenation mixed feed heat exchanger is also connected between the pre-hydrogenation feed filter and the heating furnace, the inlet and outlet ends of the cold medium flow of the pre-hydrogenation mixed feed heat exchanger are respectively connected with the pre-hydrogenation feed filter and the heating furnace through pipelines, and the inlet and outlet ends of the heat medium flow of the pre-hydrogenation mixed feed heat exchanger are respectively connected with the pre-chlorination reactor and the pre-hydrogenation product air cooler through pipelines; the upper outlet pipeline of the pre-hydrogen adding liquid separator is connected with the inlet liquid separating tank of the circulating hydrogen compressor, the upper outlet pipeline of the inlet liquid separating tank of the circulating hydrogen compressor is connected in parallel with a pipeline between the pre-hydrogenation feeding filter and the pre-hydrogenation mixing feeding heat exchanger through the pre-hydrogenation circulating hydrogen compressor, the lower outlet pipeline of the inlet liquid separating tank of the circulating hydrogen compressor is connected in parallel with the lower outlet pipeline of the pre-hydrogen adding liquid separator, and the lower outlet pipeline of the pre-hydrogen adding liquid separator is connected with the stripping tower of the reforming device; the device is characterized in that a connecting pipe line of the pre-hydrogenation mixed feeding heat exchanger and the pre-hydrogenation product air cooler is connected with a hydrogen supplementing pipeline in parallel, the hydrogen supplementing pipeline is sequentially connected with a hydrogen supplementing compressor inlet liquid separating tank and a pre-hydrogenation hydrogen supplementing compressor from front to back, and a hydrogen supplementing circulating cooler is connected with the inlet end of the hydrogen supplementing compressor inlet liquid separating tank and the outlet end of the pre-hydrogenation hydrogen supplementing compressor in parallel.
Further, a naphtha discharging pipeline of the diesel hydrogenation device is provided with a branch and is connected with a mixed naphtha tank.
The process comprises heating the mixed feed of the diesel hydrogenation device by a heating furnace, hydrotreating by a hydrofining reactor and a hydro-upgrading reactor in sequence, separating oil from gas by separators, and feeding into a stripping tower and a fractionating tower of a fractionating system, wherein the fractionating tower directly feeds the naphtha to the stripping tower of the reforming device by a naphtha feed pump.
Further, the inlet temperature of the hydro-upgrading reactor is controlled to be 320-330 ℃, the hydrogen-oil ratio is controlled to be 600-700, and the airspeed is controlled to be 0.85-0.95 and 0.95h -2 。
Further, the steam injection amount of the stripping tower of the fractionating system is controlled to be 2.5-3.2t/h.
Further, the sulfur content of the fractionator direct fed reformer stripper naphtha is controlled to be less than 0.5ppm.
Further, the straight-run naphtha from the atmospheric and vacuum device and the coker naphtha from the hydrogenation of the coker gasoline and diesel oil are firstly hydrotreated by a pre-hydrogenation unit of the reformer, and then enter a stripping tower of the reformer.
The process adopts the diesel hydrogenation device naphtha to directly supply the reforming device pre-hydrogenation unit stripping tower without passing through the existing reforming device pre-hydrogenation unit, so that compared with the prior art, the process has the advantages of shortened process flow, low energy consumption and convenient operation; meanwhile, different treatment processes can be flexibly adopted according to different qualities and sources of naphtha, and the application range of the whole system and the process is enlarged.
Drawings
FIG. 1 is a flow diagram of a diesel hydrotreater naphtha direct reformer process;
FIG. 2 is a process flow diagram of a naphtha reforming pre-hydrogenation;
in the figure: 1. a heat exchanger, 2, a heating furnace, 3, a hydrofining reactor, 4, a hydro-upgrading reactor, 5, a hot high-pressure separator, 6, a hot low-pressure separator, 7, a cold low-pressure separator, 8, a cold high-pressure separator, 9, a stripping tower, 10, a stripping tower top reflux tank, 11, a fractionating tower, 12, a fractionating tower top reflux tank, 13, a circulating hydrogen desulfurization tower, 14 and a circulating hydrogen compressor; 101. the device comprises a pre-hydrogenation feed buffer tank, 102, a pre-hydrogenation feed pump, 103, a pre-hydrogenation feed filter, 104, a pre-hydrogenation mixed feed heat exchanger, 105, a pre-hydrogenation feed heating furnace, 106, a pre-hydrogenation reactor, 107, a pre-addition dechlorination reactor, 108, a pre-hydrogenation gas-liquid separator, 109, a circulating hydrogen compressor inlet liquid separating tank, 110, a pre-hydrogenation circulating hydrogen compressor, 111, a supplementary hydrogen compressor inlet liquid separating tank, 112, a pre-hydrogenation supplementary hydrogen compressor, 113, a supplementary hydrogen circulating cooler, 114 and a pre-hydrogenation product air cooler.
Detailed Description
The invention is further described below with reference to specific examples and figures.
Example 1
Referring to fig. 1, a system of a diesel hydrogenation device naphtha direct supply reformer comprises a diesel hydrogenation device and a reformer stripper which are connected with each other, wherein the diesel hydrogenation device comprises a heat exchanger 1, a heating furnace 2, a hydrofining reactor 3, a hydro-upgrading reactor 4, a hot high pressure separator 5, a hot low pressure separator 6, a cold low pressure separator 7, a cold high pressure separator 8 and a fractionation system which are connected with each other by pipelines, and an inlet of the heating furnace 2 is connected with a diesel feeding pipeline; the fractionating system comprises a stripping tower 9 and a fractionating tower 11 which are connected in sequence, wherein a stripping tower top reflux tank 10 is arranged at the top of the stripping tower 9 and is connected through a reflux pipeline to form a stripping tower top reflux system; the top of the fractionating tower 11 is provided with a naphtha discharging pipeline, the naphtha discharging pipeline is provided with two branches, one branch is connected with a reflux tank 12 at the top of the fractionating tower and is connected with a reflux system at the top of the fractionating tower through a reflux pipeline, and the other branch is directly connected with the inlet of the stripping tower of the reforming device.
The cold medium flow of the heat exchanger 1 is connected with a diesel oil feeding pipeline, and the cold medium flow of the heat exchanger 1 is connected with a pipeline between the hydro-upgrading reactor 4 and the hot high-pressure separator 5; the diesel oil feeding pipe at the front end of the heat exchanger 1 is also connected with a filter.
The bottom outlet of the hot high-pressure separator 5 is connected with the inlet pipeline of the hot low-pressure separator 6 through a pipeline, and the top outlet is connected with the inlet pipeline of the cold high-pressure separator 8 through a pipeline; the top outlet of the hot low pressure separator 6 is connected to the inlet line of the cold low pressure separator 7; the bottom outlet of the hot low-pressure separator 6 and the bottom outlet of the cold low-pressure separator 7 are connected in parallel through pipelines and then are connected with a fractionation system, namely a stripping tower 9; the bottom outlet of the cold high-pressure separator 8 is connected in parallel with the inlet pipeline of the cold low-pressure separator 7 through a pipeline; the top outlet of the cold high-pressure separator 8 is connected with the inlet of the circulating hydrogen desulfurization tower 13 through a pipeline, the outlet of the circulating hydrogen desulfurization tower 13 is connected with the inlet of the circulating hydrogen compressor 14 through a pipeline, and the outlet pipeline of the circulating hydrogen compressor 14 is provided with branches which are respectively connected with the hydrogen inlet pipelines of the hydrofining reactor 3 and the hydro-upgrading reactor 4.
The process flow is as follows: the mixed feed of the diesel hydrogenation device is filtered by a filter, then enters a heating furnace 2 for heating after exchanging heat with a hydrogenation product by a heat exchanger 1, then is subjected to hydrogenation treatment by a hydrofining reactor 3 and a hydro-upgrading reactor 4 in sequence, then the hydrogenation product is subjected to oil-gas separation by each separator and then enters a stripping tower 9 and a fractionating tower 10 of a fractionating system, and the fractionating tower 10 directly sends the produced naphtha to a stripping tower of a reforming device by a naphtha delivery pump. And (3) process control: the inlet temperature of the modifying reactor is controlled at 320-330 ℃, the hydrogen-oil ratio is controlled at 600-700, and the airspeed is controlled at 0.85-0.95h -2 The method comprises the steps of carrying out a first treatment on the surface of the Controlling the steam injection amount of the stripping tower of the fractionating system to be 2.5-3.2t/h; the sulfur content of the direct supply naphtha is controlled to be lower than 0.5ppm.
Example 2
In order to meet the reforming treatment of naphtha with different qualities and sources, the system further comprises a reformer pre-hydrogenation unit, referring to fig. 2, on the basis of the embodiment 1, wherein the reformer pre-hydrogenation unit comprises a mixed naphtha tank, a pre-hydrogenation feed buffer tank 101, a pre-hydrogenation feed pump 102, a pre-hydrogenation feed filter 103, a pre-hydrogenation mixed feed heat exchanger 104, a pre-hydrogenation feed heating furnace 105, a pre-hydrogenation reactor 106, a pre-addition dechlorination reactor 107, a pre-hydrogenation product air cooler 114 and a pre-hydrogenation gas-liquid separator 108 which are connected in sequence through pipelines; the inlet of the mixed naphtha tank is respectively connected with a straight-run naphtha feeding pipeline from the atmospheric and vacuum device and a coker naphtha feeding pipeline from the hydrogenation of coker gasoline and diesel, and a naphtha discharging pipeline (namely a pipeline shown by the hydrogenation modification of distillate hydrogenated naphtha from diesel in fig. 2) of the diesel hydrogenation device is provided with a branch and is connected with the mixed naphtha tank; the inlet and outlet ends of the cold medium flow of the pre-hydrogenation mixed feed heat exchanger 104 are respectively connected with the pre-hydrogenation feed filter 103 and the pre-hydrogenation feed heating furnace 105 through pipelines, and the inlet and outlet ends of the heat medium flow of the pre-hydrogenation mixed feed heat exchanger 104 are respectively connected with the pre-addition dechlorination reactor 107 and the pre-hydrogenation product air cooler 114 through pipelines; the upper outlet pipeline of the pre-hydrogenation gas-liquid separator 108 is connected with the inlet liquid separating tank 109 of the circulating hydrogen compressor, the upper outlet pipeline of the inlet liquid separating tank 109 of the circulating hydrogen compressor is connected in parallel with the pipeline between the pre-hydrogenation feed filter 103 and the pre-hydrogenation mixed feed heat exchanger 104 through the pre-hydrogenation circulating hydrogen compressor 110, the lower outlet pipeline of the inlet liquid separating tank 109 of the circulating hydrogen compressor is connected in parallel with the lower outlet pipeline of the pre-hydrogenation gas-liquid separator 108, and the lower outlet pipeline of the pre-hydrogenation gas-liquid separator 108 is connected with the reformer stripper; the pre-hydrogenation mixed feeding heat exchanger 104 is connected with a hydrogen supplementing pipeline in parallel on a connecting pipe of the pre-hydrogenation product air cooler 114, the hydrogen supplementing pipeline is sequentially connected with a hydrogen supplementing compressor inlet liquid separating tank 111 and a pre-hydrogenation hydrogen supplementing compressor 112 from front to back, and a hydrogen supplementing circulating cooler 113 is connected with the inlet end of the hydrogen supplementing compressor inlet liquid separating tank 111 and the outlet end of the pre-hydrogenation hydrogen supplementing compressor 112 in parallel.
The process flow is as follows: the naphtha of the diesel hydrogenation device can be subjected to two choices according to different qualities, and directly enters the stripping tower of the reforming device when the quality is higher, and when the quality is lower, the naphtha is firstly hydrotreated by a pre-hydrogenation unit of the reforming device together with straight-run naphtha from the atmospheric and vacuum device and coked naphtha from the hydrogenation of coked gasoline and diesel, and then enters the stripping tower of the reforming device.
Compared with the prior design, namely, the naphtha of the hydro-upgrading device is directly supplied to a naphtha tank of a pre-hydrogenation unit of the reforming device, and the naphtha tank and the rest naphtha are subjected to hydro-refining and steam stripping to provide qualified raw materials of the reforming unit; according to the invention, the diesel hydro-upgrading is optimized to produce qualified reforming raw materials, and the part of naphtha directly enters the stripping tower without hydrofining, so that the raw material pump load of a reforming pretreatment unit can be reduced by 22%, the heating furnace load can be reduced by 25%, and the catalyst airspeed can be reduced by 25%. The reforming pre-hydrogenation unit saves energy by about 15 percent.
It will be readily appreciated by those skilled in the art that the foregoing description is merely a preferred embodiment of the invention and is not intended to limit the invention, but any modifications, equivalents, improvements or alternatives falling within the spirit and principles of the invention are intended to be included within the scope of the invention.
Claims (6)
1. A system for a diesel hydrogenation unit naphtha direct feed reformer, characterized by: the device comprises a diesel hydrogenation device and a reformer stripping tower which are connected with each other, wherein the diesel hydrogenation device comprises a heating furnace, a hydrofining reactor, a hydro-upgrading reactor, a hot high-pressure separator, a hot low-pressure separator, a cold low-pressure separator and a fractionating system which are connected with each other through pipelines in sequence, and an inlet of the heating furnace is connected with a diesel feeding pipeline; the fractionating system comprises a stripping tower and a fractionating tower which are sequentially connected, wherein the top of the stripping tower is provided with a reflux tank and is connected with the reflux tank through a reflux pipeline to form a top reflux system of the stripping tower; the top of the fractionating tower is provided with a naphtha discharging pipeline, the naphtha discharging pipeline is provided with two branches, one branch is connected with a reflux tank and is connected with a reflux system at the top of the fractionating tower through the reflux pipeline, and the other branch is directly connected with the inlet of the stripping tower of the reforming device;
the diesel hydrogenation device also comprises a heat exchanger, wherein the cold medium flow of the heat exchanger is connected with a diesel feeding pipeline, and the cold medium flow of the heat exchanger is connected to a pipeline between the hydro-upgrading reactor and the hot high-pressure separator; a filter is also connected to the diesel oil feed pipe at the front end of the heat exchanger;
the diesel hydrogenation device also comprises a cold high-pressure separator; the bottom outlet of the hot high-pressure separator is connected with the inlet pipeline of the hot low-pressure separator through a pipeline, and the top outlet of the hot high-pressure separator is connected with the inlet pipeline of the cold high-pressure separator through a pipeline; the top outlet of the hot low-pressure separator is connected with the inlet pipeline of the cold low-pressure separator; the bottom outlet of the hot low-pressure separator and the bottom outlet of the cold low-pressure separator are connected in parallel through pipelines and then connected with a fractionation system; the bottom outlet of the cold high-pressure separator is connected in parallel with the inlet pipeline of the cold low-pressure separator through a pipeline; the top outlet of the cold high-pressure separator is connected with the inlet of the circulating hydrogen desulfurization tower through a pipeline, the outlet of the circulating hydrogen desulfurization tower is connected with the inlet of a circulating hydrogen compressor through a pipeline, and the outlet pipeline of the circulating hydrogen compressor is provided with branches which are respectively connected with the hydrogen inlet pipelines of the hydrofining reactor and the hydro-upgrading reactor;
the system also comprises a reforming device pre-hydrogenation unit, wherein the reforming device pre-hydrogenation unit comprises a mixed naphtha tank, a pre-hydrogenation feed buffer tank, a pre-hydrogenation feed filter, a heating furnace, a pre-hydrogenation reactor, a pre-chlorination reactor, a pre-hydrogenation product air cooler and a pre-hydrogenation gas-liquid separator which are connected in sequence through pipelines; the inlet of the mixed naphtha tank is respectively connected with a straight-run naphtha feeding pipeline from the atmospheric and vacuum device and a coker naphtha feeding pipeline from the hydrogenation of coker gasoline and diesel; a pre-hydrogenation mixed feed heat exchanger is also connected between the pre-hydrogenation feed filter and the heating furnace, the inlet and outlet ends of the cold medium flow of the pre-hydrogenation mixed feed heat exchanger are respectively connected with the pre-hydrogenation feed filter and the heating furnace through pipelines, and the inlet and outlet ends of the heat medium flow of the pre-hydrogenation mixed feed heat exchanger are respectively connected with the pre-chlorination reactor and the pre-hydrogenation product air cooler through pipelines; the upper outlet pipeline of the pre-hydrogen adding liquid separator is connected with the inlet liquid separating tank of the circulating hydrogen compressor, the upper outlet pipeline of the inlet liquid separating tank of the circulating hydrogen compressor is connected in parallel with a pipeline between the pre-hydrogenation feeding filter and the pre-hydrogenation mixing feeding heat exchanger through the pre-hydrogenation circulating hydrogen compressor, the lower outlet pipeline of the inlet liquid separating tank of the circulating hydrogen compressor is connected in parallel with the lower outlet pipeline of the pre-hydrogen adding liquid separator, and the lower outlet pipeline of the pre-hydrogen adding liquid separator is connected with the stripping tower of the reforming device; the device comprises a pre-hydrogenation mixed feeding heat exchanger, a pre-hydrogenation product air cooler, a pre-hydrogenation recycle cooler and a pre-hydrogenation recycle cooler, wherein the pre-hydrogenation mixed feeding heat exchanger is connected with a connecting pipe of the pre-hydrogenation product air cooler in parallel;
and a naphtha discharging pipeline of the diesel hydrogenation device is provided with a branch and is connected with a mixed naphtha tank.
2. A process for a diesel hydro-unit naphtha direct feed reformer employing the system of claim 1, characterized by: the process flow is that the mixed feed of the diesel hydrogenation device is heated by a heating furnace, then is hydrotreated by a hydrofining reactor and a hydro-upgrading reactor in sequence, is subjected to oil-gas separation by each separator, and then enters a stripping tower and a fractionating tower of a fractionating system, and the fractionating tower directly sends the produced naphtha to the stripping tower of the reforming device by a naphtha external pump.
3. The process for a diesel hydro-unit naphtha direct fed reformer according to claim 2, wherein: the inlet temperature of the hydro-upgrading reactor is controlled to be 320-330 ℃, the hydrogen-oil ratio is controlled to be 600-700, and the airspeed is controlled to be 0.85-0.95h -2 。
4. The diesel hydro-plant naphtha direct fed reformer process of claim 2, wherein: the steam injection amount of the stripping tower of the fractionating system is controlled to be 2.5-3.2t/h.
5. The diesel hydro-plant naphtha direct fed reformer process of claim 2, wherein: the sulfur content of the fractionator direct fed reformer stripper naphtha is controlled to be less than 0.5ppm.
6. The diesel hydro-plant naphtha direct fed reformer process of any one of claims 2-5, wherein: the straight-run naphtha from the atmospheric and vacuum device and the coker naphtha from the hydrogenation of the coker gasoline and diesel oil are firstly hydrotreated by a pre-hydrogenation unit of the reformer and then enter a stripping tower of the reformer.
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| CN110228793B (en) * | 2019-07-29 | 2023-10-27 | 正和集团股份有限公司 | Direct supply process and device for reforming hydrogen used as diesel hydro-upgrading hydrogen source |
| CN113943588B (en) * | 2020-07-16 | 2022-12-02 | 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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