CN102234541B - Energy-saving pyrolysis gasoline full-cut hydrogenation method and device - Google Patents
Energy-saving pyrolysis gasoline full-cut hydrogenation method and device Download PDFInfo
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- CN102234541B CN102234541B CN 201010165197 CN201010165197A CN102234541B CN 102234541 B CN102234541 B CN 102234541B CN 201010165197 CN201010165197 CN 201010165197 CN 201010165197 A CN201010165197 A CN 201010165197A CN 102234541 B CN102234541 B CN 102234541B
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Abstract
The invention relates to an energy-saving pyrolysis gasoline full-cut hydrogenation method and a device thereof. The device provided by the invention comprises: a) a first segment hydrogenation reactor system; b) a Carbon 5 removal tower system; c) a Carbon 9 removal tower system; d) a second segment hydrogenation reactor system; and e) a stabilization tower system. Apart from a Carbon 9 removal tower bottom reboiler disposed in the Carbon 9 removal tower system, a Carbon 9 removal tower intermediate reboiler is also arranged on the upper portion of the Carbon 9 removal tower stripping section, wherein a heating medium of the Carbon 9 removal tower intermediate reboiler is a hydrogenated gasoline product collected from the stabilization tower bottom. With the adoption of the pyrolysis gasoline full-cut hydrogenation method in the invention, the consumption of steam and cooling water in the pyrolysis gasoline full-cut hydrogenation device can be obviously decreased so as to reduce the total energy consumption of the pyrolysis gasoline full-cut hydrogenation device.
Description
Skill wood field
The present invention relates to petrochemical complex pyrolysis gasoline hydrogenation field, say further, relate to a kind of pyrolysis gasoline hydrogenation of total effluent power-economizing method and device.
Background technology
Pyrolysis gasoline claims pyrolysis gasoline again.Be raw material with lighter hydrocarbons, petroleum naphtha, diesel oil even decompressed wax oil, Pintsch process is produced in the process of ethene in the presence of water vapour, generates the above liquid by-product of carbon containing five hydro carbons, and to do be that 205 ℃ liquid is called pyrolysis gasoline through fractionating out.Because this kind gasoline is rich in aromatic hydrocarbons, through can be used as high octane gasoline component after the hydrofining or being used for industrial chemicals such as benzene extraction, toluene, ethylbenzene, dimethylbenzene.
At present, industrial pyrolysis gasoline hydrogenation is refining generally all is to adopt the method for two-stage catalytic selective hydrogenation to remove a large amount of unsaturatess and the impurity that contains in the pyrolysis gasoline: monoolefine, diolefine, alkenyl arene, sulfide etc.Wherein, first section hydrogenation is under than the mitigation condition, carries out liquid phase reaction, and its hydrogenation purpose mainly is to make diolefine be converted into monoolefine, and alkenyl arene is converted into alkylaromatic hydrocarbon; Second section hydrogenation is under comparatively high temps, carries out gas-phase reaction, and its hydrogenation purpose mainly is to make monoolefine be converted into stable hydrocarbon, and sulfide is converted into H
2S.
According to the difference of products scheme, industrial application hydrofinishing process more widely can be divided into two kinds of pyrolysis gasoline heart cut hydrogenation and pyrolysis gasoline hydrogenation of total effluent.
So-called pyrolysis gasoline hydrogenation of total effluent, its device systems generally is made up of three towers, two anti-systems.Be followed successively by one-stage hydrogenation reactive system, decarburization five Tower Systems, decarburization nine Tower Systems, secondary hydrogenation reactive system and stabilizer tower system.Raw material ethylene unit by product raw pyrolysis gasoline is converted into monoene through one-stage selective hydrogenation with the diene in the raw material earlier, isolates C through decarburization five towers successively again
5And C
5Following cut, decarburization nine towers remove C
9And C
9Above cut removes C
5And C
9C behind the cut
6-C
8Cut is handled through second section selective hydrogenation monoene is converted into stable hydrocarbon, and obtains the hydrogenated gasoline product after removing sulfide.Hydrogenation of net product gasoline (C
6-C
8Cut) is mainly used in the raw material of aromatic extraction unit; As byproduct, hydrogenating carbon five products behind the one-stage hydrogenation can be used as cracking stock and return ethylene unit; Hydrogenating carbon nine products behind the one-stage hydrogenation can be done oil fuel or blended gasoline.
According to chemical principle, hydrogenation of unsaturated hydrocarbons is thermopositive reaction, and the unsaturated hydrocarbons content in the pyrolysis gasoline heart cut can be up to 50-60wt%, therefore pyrolysis gasoline heart cut hydrogenation reaction is generally strong exothermal reaction, reaction product must be handled through overcooling, flash distillation, needs to consume a large amount of heat-eliminating mediums thus.Separation column then needs to consume a large amount of steam as the heating medium of tower reactor reboiler in the pyrolysis gasoline hydrogenation flow process.Wherein, decarburization nine towers of pyrolysis gasoline hydrogenation of total effluent flow process are generally atmospheric tower, and about 190 ℃ of tower reactor temperature need working pressure to be not less than the steam of 2.2MPaG as the heating medium of tower reactor reboiler.
Along with the continuous increase of chemical industry scale, the processing power of industrialization pyrolysis gasoline hydrogenation device is increasing at present, and the device total energy consumption also increases thereupon.Under the trend of resource growing tension, the energy consumption level that reduces device becomes the major issue that needs to be resolved hurrily.
There have been decades the pyrolysis gasoline hydrogenation of total effluent method industrial application time, but its core technology is all grasped in abroad some large-scale petroleum petro-chemical corporation hands always.At present disclosed prior art rarely has and relates to the energy-conservation working method of pyrolysis gasoline hydrogenation.
Disclose the technical flow of hydrogenation of gasolene through catalytic cracking full distillate design among the CN1916119A, the improvement that it has mainly designed catalytic gasoline hydrogenation reforming technology flow process all circulates by liquid hydrocarbon, utilizes reactant and raw material technology such as heat exchange step by step.Wherein having related in the technical flow of hydrogenation of gasolene through catalytic cracking full distillate in the stabilizer tower cat head oil gas returns return tank of top of the tower through condensate cooler and carries out gas-liquid separation, gas phase acts as a fuel and enters gas train, a liquid phase part is returned cat head and is done backflow, another part returns feed gasoline, a liquid phase part refluxes another part and stabilizer tower charging heat exchange at the bottom of the tower through reboiler.This method is at catalytic cracking process energy optimizing method and measure, and because there is notable difference in the pyrolysis gasoline of the raw material of catalytic cracking process and raw material ethylene unit by-product involved in the present invention, cause the operational path of catalytic cracking full distillate gasoline hydrogenation and pyrolysis gasoline hydrogenation of total effluent to have essential distinction.Therefore, the disclosed concrete optimization method of this method and measure are only applicable to hydrocracking process, the optimization of the pyrolysis gasoline hydrogenation of total effluent flow process that the present invention relates to are not possessed the technology enlightenment of apparent property.
By the analysis to pyrolysis gasoline hydrogenation of total effluent prior art, the contriver finds that some high-temperature technology logistics are arranged in the pyrolysis gasoline hydrogenation of total effluent flow process, and its heat is not fully used, and has energy-optimised possibility.
Summary of the invention
At the problem that prior art exists, the whole process logistics is being carried out on the basis of energy-optimised analysis and research, the contriver optimizes by a series of flow process adjustment, can realize that the consumption of heating steam and heat-eliminating medium reduces greatly.The contriver utilizes commercial flowsheeting software, independent research pyrolysis gasoline hydrogenation of total effluent simulator program, by optimization design and the test to the pyrolysis gasoline hydrogenation flow process, proposed a kind of new pyrolysis gasoline hydrogenation of total effluent method and apparatus, the existing pyrolysis gasoline hydrogenation technology of consumption rate of heating steam and heat-eliminating medium is reduced greatly.
One of the present invention's pyrolysis gasoline heart cut method of hydrotreating is achieved in that
The raw material raw pyrolysis gasoline of the method for the invention passes through a) one-stage hydrogenation reactor assembly, b successively) decarburization five Tower Systems, c) decarburization nine Tower Systems, d) secondary hydrogenation reactor assembly, e) the stabilizer tower system, obtain the hydrogenated gasoline product; It is characterized in that:
Described decarburization nine Tower Systems also arrange decarburization nine tower intermediate reboilers on decarburization nine tower stripping section tops except decarburization nine Tata still reboilers are set, the heating medium of these decarburization nine tower intermediate reboilers is the hydrogenated gasoline product of stabilizer tower tower reactor extraction.
In concrete enforcement,
The hydrogenated gasoline product of described stabilizer tower tower reactor extraction is earlier with delivering to decarburization nine tower intermediate reboilers as the heating medium of decarburization nine tower intermediate reboilers after the pressurization of hydrogenated gasoline product pump, deliver to stabilizer tower input and output material interchanger again preheating is carried out in the stabilizer tower charging, the last storing temp that is cooled to the hydrogenated gasoline product requirement again through the hydrogenated gasoline water cooler;
The liquid phase feeding of described decarburization nine tower intermediate reboilers can be by any plate extraction in the 3rd～6 block of plate of decarburization nine tower stripping sections, and 115～125 ℃ of extraction temperature are returned second block of column plate under the extraction plate after the vaporization;
Described decarburization nine tower intermediate reboiler vaporization rate are 10～15wt%, and thermal load is 10～15% of decarburization nine Tata still reboiler thermal loads;
Described decarburization nine tower working pressures are negative pressure, and tower top temperature is 65～75 ℃, and the tower reactor temperature is 135～150 ℃;
Described stabilizer tower feeding temperature≤135 ℃, tower reactor temperature are 150～170 ℃.
In concrete enforcement
Pyrolysis gasoline hydrogenation of total effluent method of the present invention is characterized in that described method can comprise successively:
A) one-stage hydrogenation reactor assembly
Raw pyrolysis gasoline enters a section feeding surge tank after filtering through raw gasline charging strainer, boosts through the one-stage hydrogenation fresh feed pump then, and enters one-stage hydrogenation reactor top after one section recycle stock mixes; Hydrogen has the introducing of hydrogen pipe network to send into the one-stage hydrogenation reactor head;
The discharging of one-stage hydrogenation reactor enters the flash distillation of one-stage hydrogenation hot knock-out pot, and the gas phase part enters the cold separating tank of one-stage hydrogenation behind one section thermal separation condenser, and isolated gas phase is sent to two sections circulating hydrogen compressor suction tanks; Liquid phase part returns the one-stage hydrogenation hot knock-out pot, the liquid part of one-stage hydrogenation hot knock-out pot bottom is through the one-stage hydrogenation recycle pump, deliver to one section back raw pyrolysis gasoline of sending here with the one-stage hydrogenation fresh feed pump of recirculation cooler cooling and be mixed into the one-stage hydrogenation reactor head, another part enters decarburization five towers middle part;
B) decarburization five Tower Systems
Decarburization five top of tower gas phases enter decarburization five tower return tanks behind decarburization five column overhead condensers, decarburization five tower return tank dischargings are returned decarburization five tops of tower through decarburization five tower reflux pump parts, and another part is sent to carbon five product storage tanks; Decarburization five Tata still dischargings enter decarburization nine towers middle part;
Decarburization five towers are provided with decarburization five Tata still reboilers;
C) decarburization nine Tower Systems
Decarburization nine top of tower gas phases enter decarburization nine tower return tanks behind decarburization nine column overhead condensers, decarburization nine tower return tank discharging parts are returned decarburization nine tops of tower through decarburization nine tower reflux pumps, and another part is delivered to two sections input and output material interchanger through the secondary hydrogenation fresh feed pump;
Decarburization nine Tata still dischargings send carbon nine product storage tanks after the cooling of carbon nine tower reactor product coolers through decarburization nine Tata still pumps again;
Decarburization nine towers also are provided with decarburization nine tower intermediate reboilers except decarburization nine Tata still reboilers are set;
D) secondary hydrogenation reactor assembly
After the recycle hydrogen of material from the secondary hydrogenation fresh feed pump with two sections circulating hydrogen compressors mixes, after two sections input and output material interchanger and the heating of two section feeding process furnace, enter the secondary hydrogenation reactor head successively; The second stage reactor bottom discharge through two sections input and output material interchanger, two sections aftercoolers, is delivered to the secondary hydrogenation separating tank successively, and the isolated gas phase of secondary hydrogenation separating tank is sent two sections circulating hydrogen compressor suction tanks; Two sections circulating hydrogen compressor suction tank gas phases are sent two sections input and output material heat exchanger entrances after two sections circulating hydrogen compressors boost.The secondary hydrogenation separating tank is isolated liquid phase and is entered stabilizer tower input and output material interchanger;
E) stabilizer tower system
The liquid phase of secondary hydrogenation separating tank enters the stabilizer tower middle part through the heating of stabilizer tower input and output material interchanger; Stabilizer tower cat head gas phase enters the stabilizer tower return tank through the stabilizer tower overhead condenser, and stabilizer tower return tank gas phase is sent the low-pressure tail gas pipe network, and liquid phase is returned the stabilizer tower cat head through the pressurization of stabilizer tower reflux pump; The discharging of stabilizer tower tower reactor is boosted through the hydrogenated gasoline product pump, after decarburization nine tower intermediate reboilers, stabilizer tower input and output material interchanger and the cooling of hydrogenated gasoline reactor product cooler, send hydrogenated gasoline product storage tank successively.
The present invention's two pyrolysis gasoline hydrogenation of total effluent device is achieved in that
Pyrolysis gasoline hydrogenation of total effluent device of the present invention comprises:
A) one-stage hydrogenation reactor R-750 system, b) decarburization five tower C-710 systems, c) decarburization nine tower C-720 systems, d) secondary hydrogenation reactor R-760 system, e) stabilizer tower C-770 system; It is characterized in that:
Described decarburization nine tower C-720 also arrange decarburization nine tower intermediate reboiler E-726 on decarburization nine tower C-720 stripping section tops except decarburization nine Tata still reboiler E-725 are set in tower reactor;
The entrance of described decarburization nine tower intermediate reboiler E-726 heating mediums is connected with hydrogenated gasoline product pump P-775 outlet, and hydrogenated gasoline product pump P-775 entrance is connected with the outlet of stabilizer tower C-770 tower reactor through pipeline;
The outlet of described decarburization nine tower intermediate reboiler E-726 heating mediums is connected with the import of stabilizer tower input and output material interchanger E-776 thermal medium.
In concrete enforcement,
Described device comprises following equipment successively:
A) one-stage hydrogenation reactor R-750 system
The raw pyrolysis gasoline raw material connects following equipment by raw pyrolysis gasoline storage tank TK-700 successively through pipeline: raw gasline charging strainer SR-700, a section feeding surge tank D-750, one-stage hydrogenation fresh feed pump P-750, and one-stage hydrogenation fresh feed pump P-750 outlet is connected to one-stage hydrogenation reactor R-750 top through pipeline;
Hydrogen gas lines is connected to one-stage hydrogenation reactor R-750 top by the hydrogen pipe network through pipeline;
One-stage hydrogenation reactor R-750 outlet at bottom connects one-stage hydrogenation hot knock-out pot D-751 through pipeline, and wherein: one-stage hydrogenation hot knock-out pot D-751 tank deck gaseous phase outlet connects one section thermal separation condenser E-752 and the cold separating tank D-752 of one-stage hydrogenation successively through pipeline; The liquid phase outlet connects one-stage hydrogenation recycle pump P-751 entrance and decarburization five tower C-710 middle part opening for feed respectively through pipeline at the bottom of the one-stage hydrogenation hot knock-out pot D-751 jar; One-stage hydrogenation recycle pump P-751 outlet is connected to through pipeline: one section recirculation cooler E-751 thermal medium entrance; One section recirculation cooler E-751 thermal medium outlet is connected to one-stage hydrogenation reactor R-750 top through pipeline;
The cold separating tank D-752 of one-stage hydrogenation top gaseous phase outlet connects two sections circulating hydrogen compressor suction tank D-761 through pipeline; The liquid phase outlet connects one-stage hydrogenation hot knock-out pot D-751 through pipeline at the bottom of the cold separating tank D-752 of the one-stage hydrogenation jar;
B) decarburization five tower C-710 systems
Decarburization five tower C-710 cat head gaseous phase outlets connect following equipment successively through pipeline: decarburization five column overhead condenser E-710, decarburization five tower return tank D-710, decarburization five tower reflux pump P-715;
Decarburization five tower reflux pump P-715 outlet connects respectively through pipeline: decarburization five tower C-710 top refluxing openings, carbon five product storage tank TK-710 opening for feeds;
The outlet of decarburization five tower C-710 tower reactor liquid phases connects decarburization nine tower C-720 middle part opening for feed through pipeline;
Decarburization five tower C-710 tower reactor reboiler extraction mouths are connected to the cold medium import of decarburization five Tata still reboiler E-715 through pipeline, and the cold media outlet of decarburization five Tata still reboiler E-715 is connected to decarburization five tower C-710 tower reactor reboiler return ports through pipeline;
C) decarburization nine tower C-720 systems
Decarburization nine tower C-720 cat head gaseous phase outlets connect following equipment successively through pipeline: decarburization nine column overhead condenser E-720, decarburization nine tower return tank D-720;
The liquid phase outlet connects decarburization nine tower reflux pump P-720 entrances and secondary hydrogenation fresh feed pump P-721 entrance respectively through pipeline at the bottom of the decarburization nine tower return tank D-720 jars; Decarburization nine tower reflux pump P-720 outlet connects decarburization nine tower C-720 top refluxing openings through pipeline; Secondary hydrogenation fresh feed pump P-721 outlet is connected to two sections cold medium imports of input and output material interchanger E-760 through pipeline;
Decarburization nine tower return tank D-720 tank deck gas phase pipelines connect decarburization nine tower tail gas condenser E-721 thermal medium imports; The outlet of decarburization nine tower tail gas condenser E-721 thermal medium liquid phases connects decarburization nine tower return tank D-720 through pipeline, and decarburization nine tower tail gas condenser E-721 thermal medium gaseous phase outlets connect the entrance of decarburization nine tower vacuum system PA-720 through pipeline; The outlet of decarburization nine tower vacuum system PA-720 is connected to vacuum tail gas pipe network through pipeline;
Decarburization nine tower C-720 tower reactors connect following equipment successively through pipeline: decarburization nine Tata still pump P-725, carbon nine reactor product cooler E-728, carbon nine product storage tank TK-720;
Decarburization nine tower C-720 tower reactor reboiler extraction mouths are connected to the cold medium import of decarburization nine Tata still reboiler E-725 through pipeline, and the cold media outlet of decarburization nine Tata still reboiler E-725 is connected to decarburization nine tower C-720 tower reactor reboiler return ports through pipeline;
Decarburization nine tower C-720 intermediate reboiler extraction mouths are connected to the cold medium import of decarburization nine tower intermediate reboiler E-726 through pipeline, and the cold media outlet of decarburization nine tower intermediate reboiler E-726 is connected to decarburization nine tower C-720 intermediate reboiler return ports through pipeline;
D) secondary hydrogenation reactor R-760 system
Two sections cold media outlets of input and output material interchanger E-760 are connected to the cold medium import of two section feeding process furnace F-760 through pipeline, and the cold medium import of two section feeding process furnace F-760 is connected to secondary hydrogenation reactor R-760 top inlet through pipeline;
Secondary hydrogenation reactor R-760 outlet at bottom is connected to two sections input and output material interchanger E-760 thermal medium entrances through pipeline; Two sections input and output material interchanger E-760 thermal medium outlets are connected to two sections aftercondenser E-761 thermal medium entrances respectively through pipeline; Two sections aftercondenser E-761 thermal medium outlets are connected to secondary hydrogenation separating tank D-760 import;
The gaseous phase outlet at secondary hydrogenation separating tank D-760 top is connected to two sections circulating hydrogen compressor suction tank D-761 through pipeline; Two sections circulating hydrogen compressor suction tank D-761 top gaseous phase outlets are connected to two sections circulating hydrogen compressor K-760 entrances through pipeline; Two sections circulating hydrogen compressor K-760 outlet is connected to connection line between secondary hydrogenation fresh feed pump P-721 and two sections input and output material interchanger E-760 through pipeline;
The outlet of secondary hydrogenation separating tank D-760 bottom liquid phases is connected to the cold medium import of stabilizer tower input and output material interchanger E-776 through pipeline;
E) stabilizer tower C-770 system
The cold media outlet of stabilizer tower input and output material interchanger E-776 is connected to stabilizer tower C-770 middle part opening for feed through pipeline;
Stabilizer tower C-770 overhead line connects successively: stabilizer tower overhead condenser E-770, stabilizer tower return tank D-770; The liquid phase outlet is connected to stabilizer tower reflux pump P-770 entrance through pipeline at the bottom of the stabilizer tower return tank D-770 jar; Stabilizer tower reflux pump P-770 outlet is connected to stabilizer tower C-770 trim the top of column mouth through pipeline; Stabilizer tower return tank D-770 tank deck gaseous phase outlet is connected to the low-pressure tail gas pipe network through pipeline;
Stabilizer tower C-770 tower reactor discharge port is connected to hydrogenated gasoline product pump P-775 entrance through pipeline; Hydrogenated gasoline product pump P-775 outlet is connected to decarburization nine tower intermediate reboiler E-726 thermal medium entrances through pipeline; The outlet of decarburization nine tower intermediate reboiler E-726 thermal mediums is connected to stabilizer tower input and output material interchanger E-776 thermal medium entrance through pipeline; The outlet of stabilizer tower input and output material interchanger E-776 thermal medium is connected to hydrogenated gasoline water cooler E-777 thermal medium entrance through pipeline; The outlet of hydrogenated gasoline water cooler E-777 thermal medium is connected to hydrogenated gasoline product storage tank TK-770 through pipeline;
Stabilizer tower C-770 tower reactor reboiler extraction mouth is connected to the cold medium import of stabilizer tower tower reactor reboiler E-775 through pipeline, and the cold media outlet of stabilizer tower tower reactor reboiler E-775 is connected to stabilizer tower C-770 tower reactor reboiler return port through pipeline.
Technical process of the present invention is compared with existing pyrolysis gasoline hydrogenation of total effluent flow process, and flow change is mainly reflected in the following aspects:
1) decarburization nine towers change vacuum column into by atmospheric tower;
2) except decarburization nine Tata still reboilers, increased decarburization nine tower intermediate reboilers, the charging of decarburization nine tower intermediate reboilers is the liquid phase material of any plate extraction in the 3rd～6 block of column plate under the decarburization nine tower opening for feeds; Liquid phase material becomes gas-liquid two-phase after decarburization nine tower intermediate reboilers heating vaporization, returns on second block of column plate of decarburization nine tower intermediate reboiler extraction column plates below; The vaporization rate that decarburization nine tower reboilers return decarburization nine tower materials is 10～15wt%.
3) thermal load of decarburization nine tower intermediate reboilers when not adding decarburization nine tower intermediate reboilers former decarburization nine Tata still reboiler thermal loads 10～15%.
4) decarburization nine tower intermediate reboilers adopt the thermal process material of stabilizer tower tower reactor extraction as heating medium; This heating medium by the extraction of stabilizer tower tower reactor after, after the pressurization of the hydrogenated gasoline product pump of stabilizer tower tower reactor, be sent to decarburization nine tower intermediate reboilers again as heating medium; After decarburization nine tower intermediate reboiler heat exchange, this heating medium is delivered to stabilizer tower input and output material interchanger again and is used for the charging of heating stabilizer tower, afterwards through delivering to the hydrogenated gasoline storage tank after the cooling of hydrogenated gasoline water cooler.
After the optimization by above-mentioned several aspects, compare with existing pyrolysis gasoline hydrogenation of total effluent method, the energy-saving effect that the present invention can realize is mainly reflected in the following aspects:
1) decarburization nine towers change vacuum column into by atmospheric tower, can make this Tata still temperature be reduced to 140～150 ℃ by 190～200 ℃, therefore the heating medium of decarburization nine Tata still reboilers can correspondingly adopt the middle pressure steam of lower pressure grade, can reduce running cost so on the one hand, simultaneously because the reduction of the steam grade of using, decarburization nine Tata still reboilers and vapour line can the junior material manufacturings of working pressure, can further reduce equipment, the pipeline investment of device thus.
2) behind the increase decarburization nine tower intermediate reboilers, decarburization nine Tata still reboiler thermal loads will reduce about 10～15%, and namely the steam energy consumption reduces about 10～15%.
3) as the pyrolysis gasoline hydrogenation of total effluent method of prior art, its stabilizer tower tower reactor discharging is sent hydrogenated gasoline product storage tank after going through twice heat exchange of stabilizer tower input and output material interchanger and hydrogenated gasoline reactor product cooler usually.According to method of the present invention, the discharging of stabilizer tower tower reactor needs successively through being sent to hydrogenated gasoline product storage tank again after decarburization nine tower intermediate reboilers, stabilizer tower input and output material interchanger and three heat exchange of hydrogenated gasoline reactor product cooler.Owing to increased the heat exchange of decarburization nine tower intermediate reboilers, under stabilizer tower input and output material exchanger heat is loaded constant prerequisite, the thermal medium temperature in of hydrogenated gasoline reactor product cooler will reduce about 40 ℃, cause the thermal load of hydrogenated gasoline water cooler to lower more than 70% thus, heat-eliminating medium consumption is also with corresponding decline more than 70%.
Heat-eliminating medium recited above can be water or air.
Description of drawings
Fig. 1 prior art pyrolysis gasoline hydrogenation of total effluent traditional process
Fig. 2 pyrolysis gasoline hydrogenation of total effluent of the present invention flow process
Description of reference numerals
1) equipment code name explanation
| The equipment code name | Device name |
| C-710 | Decarburization five towers |
| C-720 | Decarburization nine towers |
| C-770 | Stabilizer tower |
| D-710 | Decarburization five tower return tanks |
| D-720 | Decarburization nine tower return tanks |
| D-750 | One section feeding surge tank |
| D-751 | The one-stage hydrogenation hot knock-out pot |
| D-752 | The cold separating tank of one-stage hydrogenation |
| D-760 | The secondary hydrogenation separating tank |
| D-761 | Two sections circulating hydrogen compressor suction tanks |
| D-770 | The stabilizer tower return tank |
| E-710 | Decarburization five column overhead condensers |
| E-715 | Decarburization five Tata still reboilers |
| E-720 | Decarburization nine column overhead condensers |
| E-721 | Decarburization nine tower tail gas condensers |
| E-725 | Decarburization nine Tata still reboilers |
| E-726 | Decarburization nine tower intermediate reboilers |
| E-728 | Carbon nine reactor product coolers |
| E-751 | One section recirculation cooler |
| E-752 | One section thermal separation condenser |
| E-760 | Two sections input and output material interchanger |
| E-761 | Two sections aftercoolers |
| E-770 | The stabilizer tower overhead condenser |
| E-775 | Stabilizer tower tower reactor reboiler |
| E-776 | Stabilizer tower input and output material interchanger |
| E-777 | The hydrogenated gasoline water cooler |
| F-760 | Two section feeding process furnace |
| K-760 | Two sections circulating hydrogen compressors |
| P-700 | Decarburization five tower fresh feed pumps |
| P-715 | Decarburization five tower reflux pumps |
| P-720 | Decarburization nine tower reflux pumps |
| P-721 | The secondary hydrogenation fresh feed pump |
| P-725 | Decarburization nine Tata still pumps |
| P-750 | The one-stage hydrogenation fresh feed pump |
| P-751 | The one-stage hydrogenation recycle pump |
| P-770 | The stabilizer tower reflux pump |
| P-775 | The hydrogenated gasoline product pump |
| PA-720 | Decarburization nine tower vacuum systems |
| R-750 | The one-stage hydrogenation reactor |
| R-760 | The secondary hydrogenation reactor |
| SR-700 | The raw pyrolysis gasoline strainer |
| TK-700 | The raw pyrolysis gasoline storage tank |
| TK-710 | Carbon five product storage tanks |
| TK-720 | Carbon nine product storage tanks |
| TK-770 | Hydrogenated gasoline product storage tank |
2) logistics code name explanation
| The logistics code name | The logistics title |
| 1 | |
| 2 | Hydrogen |
| 3 | Hydrogenated gasoline |
| 4 | C 5Cut |
| 5 | C 9Cut |
| 6 | High |
| 7 | Low-pressure tail gas |
| 8 | Vacuum tail gas |
Embodiment
Idiographic flow is referring to accompanying drawing 2.Process description is as follows:
A) one-stage hydrogenation reactor R-750 system
From the next raw pyrolysis gasoline of raw pyrolysis gasoline storage tank TK-700, leave standstill dehydration through raw gasline charging strainer SR-700 filtration and a section feeding surge tank D-750 earlier, P-750 boosts by the one-stage hydrogenation fresh feed pump, delivers to one-stage hydrogenation reactor R-750 top after the one-stage hydrogenation recycle stock with one section recirculation cooler E-751 mixes.Hydrogen enters one-stage hydrogenation reactor R-750 from the top.
One-stage hydrogenation reactor R-750 discharging is introduced into one-stage hydrogenation hot knock-out pot D-751 and carries out gas-liquid separation.One-stage hydrogenation hot knock-out pot D-751 tank deck gas phase enters the cold separating tank D-752 of one-stage hydrogenation and carries out gas-liquid separation after one section thermal separation condenser E-752 is condensed to 43 ℃.The gas of the cold separating tank D-752 of one-stage hydrogenation tank deck is sent to two sections circulating hydrogen compressor suction tank D-761, for secondary hydrogenation provides hydrogen make-up.Liquid phase at the bottom of the cold separating tank D-752 of the one-stage hydrogenation jar is returned one-stage hydrogenation hot knock-out pot D-751 jar.A liquid phase part is through sending one-stage hydrogenation reactor R-750 back to successively as the one-stage hydrogenation recycle stock at the bottom of the one-stage hydrogenation hot knock-out pot D-751 jar after one-stage hydrogenation recycle pump P-751 pressurization and one section recirculation cooler E-751 cooling, and another part is sent to decarburization five tower C-710 middle part as the one-stage hydrogenation product.
B) decarburization five tower C-710 systems
Decarburization five column overhead gas phases are C
5Cut after decarburization five column overhead condenser E-710 are condensed to 43 ℃, enters decarburization five tower return tank D-710, returns decarburization five tower C-710 cats head through decarburization five tower reflux pump P-710 parts as backflow again; Another part is as C
5The cut byproduct is sent to carbon five product storage tank TK-710.Decarburization five tower C-710 tower reactors are C
6Above cut is sent into decarburization nine tower C-720.Decarburization five tower C-710 tower reactors are established decarburization five Tata still reboiler E-715, and heating medium is middle pressure-off superheated vapour.
C) decarburization nine tower C-720 systems
Because decarburization nine tower C-720 adopt negative-pressure operation, the tower reactor temperature is reduced to 135～150 ℃, and the heating steam of decarburization this moment nine Tata still reboiler E-725 can be adopted the middle pressure-off superheated vapo(u)r of conventional pressure rating.
Decarburization nine tower C-720 cat head gas phases are C
6～C
8Cut enters decarburization nine tower return tank D-720 after decarburization nine column overhead condenser E-720 condensations.Decarburization nine tower return tank D-720 liquid phase parts are returned decarburization nine tower C-720 cats head through decarburization nine tower reflux pump P-720 as backflow, and another part is delivered to two sections input and output material interchanger E-760 through secondary hydrogenation fresh feed pump P-721.Decarburization nine tower return tank D-720 tank deck gas phases are through decarburization nine tower tail gas condenser E-721 condensations, and the lime set of recovery is returned decarburization nine tower return tank D-720; The condensed gas phase of decarburization nine tower tail gas condenser E-721 is non-condensable gas and a small amount of hydro carbons, extracts out through decarburization nine tower pumped vacuum systems PA-720 and send vacuum tail gas pipe network.
Decarburization nine tower C-720 tower reactor materials are C
9And above cut, be sent to carbon nine reactor product cooler E-728 through decarburization nine tower reactor pump P-725 and be cooled to 43 ℃, as hydrogenation C not
9Byproduct is sent to carbon nine product storage tanks.Decarburization nine tower C-720 tower reactors are established tower reactor decarburization nine tower reboilers, and its heating medium is middle pressure-off superheated vapour.In addition, decarburization nine tower stripping section tops arrange decarburization nine tower intermediate reboiler E-726, and its heating medium is stabilizer tower C-770 tower reactor extraction and the hydrogenated gasoline after hydrogenated gasoline product pump P-775 pressurization.
D) secondary hydrogenation reaction R-760 system
The C of decarburization nine tower C-720 cats head
6～C
8Cut boosts through secondary hydrogenation fresh feed pump P-721, after the recycle hydrogen that comes from two sections circulating hydrogen compressor K-760 mixes, through two sections input and output material interchanger E-760 and two section feeding process furnace F-760 heating, delivers to secondary hydrogenation reactor R-760 top successively.
Secondary hydrogenation reactor R-760 discharging after two sections input and output material interchanger E-760 and two sections aftercooler E-761 cooling, is delivered to secondary hydrogenation separating tank D-760 and is carried out gas-liquid separation successively.The isolated gas phase major part of secondary hydrogenation separating tank D-760 enters two sections circulating hydrogen compressor suction tank D-761, and small part is discharged into the high pressure exhaust gas pipe network as high pressure exhaust gas.The gas phase of two sections circulating hydrogen compressor suction tank D-761 enters two sections circulating hydrogen compressor K-760, the C behind the one-stage hydrogenation that the gas of two sections circulating hydrogen compressor outlets and secondary hydrogenation fresh feed pump P-721 come
6-C
8Cut mixes the charging as secondary hydrogenation reactor R-760.
The isolated liquid phase discharging of secondary hydrogenation separating tank D-760 is sent to stabilizer tower C-770 then through stabilizer tower input and output material interchanger E-776 and stabilizer tower C-770 still discharging heat exchange.
E) stabilizer tower C-770 system
The liquid phase of secondary hydrogenation separating tank D-760 is sent into the middle part of stabilizer tower C-770 after stabilizer tower input and output material interchanger E-776 preheating.Stabilizer tower C-770 cat head gas phase is sent into stabilizer tower return tank D-770 after stabilizer tower overhead condenser E-770 condensation.The gas phase sulfide hydrogen of stabilizer tower return tank D-770 is sent to the low-pressure tail gas pipe network as low-pressure tail gas; The liquid phase of stabilizer tower return tank D-770 is sent stabilizer tower C-770 cat head back to through stabilizer tower reflux pump P-770.
The discharging of stabilizer tower C-770 tower reactor is the hydrogenated gasoline product, after hydrogenated gasoline product pump P-775 boosts, deliver to decarburization nine tower intermediate reboiler E-726 as the heating medium of this intermediate reboiler, deliver to the charging of the stabilizer tower C-770 of stabilizer tower input and output material interchanger E-776 again and carry out preheating, last be sent to hydrogenated gasoline product storage tank TK-770 after being cooled to the storing temp of hydrogenated gasoline product requirement through hydrogenated gasoline water cooler E-777 again.
Embodiment
Below in conjunction with embodiment, further specify the present invention.
Except decarburization nine Tower Systems, the technological design condition that pyrolysis gasoline hydrogenation of total effluent method of the present invention adopts is with existing conventional pyrolysis gasoline hydrogenation of total effluent method basically identical, and wherein the process conditions of nucleus equipment is as follows:
The main technique operational condition is as follows:
The operational condition of decarburization five tower C-710
| The position | Service temperature/℃ | Working pressure/MPaG |
| Cat head | 50～60 | 0.1～0.2 |
| Tower reactor | 125～132 |
The operational condition of decarburization nine tower C-720
| The position | Service temperature/℃ | Working pressure/MPaG |
| Cat head | 65～75 | -0.06～-0.08 |
| Tower reactor | 135～150 |
The operational condition of one-stage hydrogenation reactor R-750
The operational condition of secondary hydrogenation reactor R-760
The operational condition of stabilizer tower C-770
| The position | Service temperature/℃ | Working pressure/MPaG |
| Cat head | 105～115 | 0.5～0.55 |
| Tower reactor | 150～170 |
The raw material of pyrolysis gasoline hydrogenation is the raw pyrolysis gasoline of ethylene by-product and since the fluctuation of the raw material of ethylene unit and operation fluctuation tend to cause raw pyrolysis gasoline is formed and output than great fluctuation process.Therefore, need rationally set the unit scale of pyrolysis gasoline hydrogenation usually according to the treatment scale of ethylene unit.The scale of present newly-built ethylene unit mainly contains 800,000 tons/year, 1,000,000 tons/year and 1,200,000 tons/year, and the project scale of the pyrolysis gasoline hydrogenation device supporting with it is respectively: 550,000 tons/year, 650,000 tons/year and 800,000 tons/year.
Because it is different with operational condition and different with ethylene raw that pyrolysis gasoline is formed, and consists of the basis at this with a certain more typical raw pyrolysis gasoline and be illustrated:
C
5 -：21.5wt％
C
6-C
8：66.1wt％
C
9 +：12.4wt％
Under above-mentioned composition condition, according to two kinds of flow processs shown in accompanying drawing 1 and the accompanying drawing 2, respectively the pyrolysis gasoline hydrogenation of total effluent device of 550,000 tons/year, 650,000 tons/year and 800,000 tons of/year three kinds of scales is simulated, according to analog result, compared with prior art, the cooling water consumption that the energy-saving effect of device of the present invention is mainly reflected in two sections aftercoolers and hydrogenated gasoline water cooler reduces, specifically shown in table 1-1, table 2-1 and table 3-1; And the minimizing of decarburization nine Tata still reboiler steam energy consumptions, specifically shown in table 1-2, table 2-2 and table 3-3.
Wherein, the pressure of prior art and decarburization of the present invention nine Tata still reboiler heating steams is respectively 2.5MPaA and 1.5MPaA.Cooling water return is pressed 0.2MPaG, 43 ℃; Supply water and press 0.45MPaG, 33 ℃ of meters.Stipulate (GB/T50441-2007) that according to " petrochemical complex design energy consumption calculation standard " pressure is that the energy reduced value of the steam of 2.5MPaA and 1.5MPaA is got 3559MJ/t and 3349MJ/t respectively, the energy reduced value of recirculated cooling water is got 4.19MJ/t.
The full cut device of table ten thousand tons of/year pyrolysis gasoline hydrogenations of 1-155
Adopt the water coolant energy consumption of two kinds of devices relatively
The full cut device of table ten thousand tons of/year pyrolysis gasoline hydrogenations of 1-255
Adopt the steam energy consumption of two kinds of devices relatively
Ten thousand tons of/year pyrolysis gasoline hydrogenation of total effluent of table 2-165 device
Adopt the water coolant energy consumption of two kinds of devices relatively
The full cut device of table ten thousand tons of/year pyrolysis gasoline hydrogenations of 2-265
Adopt the steam energy consumption of two kinds of devices relatively
Ten thousand tons of/year pyrolysis gasoline hydrogenation of total effluent of table 3-180 device
Adopt the water coolant energy consumption of two kinds of devices relatively
The full cut device of table ten thousand tons of/year pyrolysis gasoline hydrogenations of 3-280
Adopt the steam energy consumption of two kinds of devices relatively
From The above results as can be seen, for the pyrolysis gasoline hydrogenation of total effluent device of different scales, adopt the total steam of device after the pyrolysis gasoline hydrogenation method of the present invention and the energy consumption of water coolant on average can reduce more than 5%.
Claims (9)
1. pyrolysis gasoline hydrogenation of total effluent method, the raw material raw pyrolysis gasoline of described method passes through a) one-stage hydrogenation reactor assembly, b successively) decarburization five Tower Systems, c) decarburization nine Tower Systems, d) secondary hydrogenation reactor assembly, e) the stabilizer tower system, obtain the hydrogenated gasoline product; It is characterized in that:
Described decarburization nine Tower Systems also arrange decarburization nine tower intermediate reboilers on decarburization nine tower stripping section tops except decarburization nine Tata still reboilers are set, the heating medium of these decarburization nine tower intermediate reboilers is the hydrogenated gasoline product of stabilizer tower tower reactor extraction.
2. pyrolysis gasoline hydrogenation of total effluent method as claimed in claim 1 is characterized in that:
The hydrogenated gasoline product of described stabilizer tower tower reactor extraction is earlier with delivering to decarburization nine tower intermediate reboilers as the heating medium of this intermediate reboiler after the pressurization of hydrogenated gasoline product pump, deliver to stabilizer tower input and output material interchanger again preheating is carried out in the stabilizer tower charging, the last storing temp that is cooled to the hydrogenated gasoline product requirement again through the hydrogenated gasoline water cooler.
3. pyrolysis gasoline hydrogenation of total effluent method as claimed in claim 2 is characterized in that:
The liquid phase feeding of described decarburization nine tower intermediate reboilers is by any plate extraction in the 3rd～6 block of column plate under the opening for feed of decarburization nine towers middle parts, and 115～125 ℃ of extraction temperature are returned second block of column plate under the extraction plate after the vaporization;
Described decarburization nine tower intermediate reboiler vaporization rate are 10～15wt%, and its thermal load is 10～15% of decarburization nine Tata still reboiler thermal loads.
4. pyrolysis gasoline hydrogenation of total effluent method as claimed in claim 2 is characterized in that:
Described decarburization nine tower working pressures are negative pressure, and tower top temperature is 65～75 ℃, and the tower reactor temperature is 135～150 ℃.
5. pyrolysis gasoline hydrogenation of total effluent method as claimed in claim 2 is characterized in that:
Described stabilizer tower feeding temperature≤135 ℃, tower reactor temperature are 150～170 ℃.
6. pyrolysis gasoline hydrogenation of total effluent method as claimed in claim 3 is characterized in that:
Described decarburization nine tower working pressures are negative pressure, and tower top temperature is 65～75 ℃, and the tower reactor temperature is 135～150 ℃;
Described stabilizer tower feeding temperature≤135 ℃, tower reactor temperature are 150～170 ℃.
7. as the described pyrolysis gasoline hydrogenation of total effluent of one of claim 1～6 method, it is characterized in that described method comprises successively:
A) one-stage hydrogenation reactive system
Raw pyrolysis gasoline enters a section feeding surge tank after filtering through raw gasline charging strainer, boosts through the one-stage hydrogenation fresh feed pump then, and enters one-stage hydrogenation reactor top after one section recycle stock mixes; Hydrogen is introduced by the hydrogen pipe network, sends into the one-stage hydrogenation reactor head;
The discharging of one-stage hydrogenation reactor enters the flash distillation of one-stage hydrogenation hot knock-out pot, and the gas phase part enters the cold separating tank of one-stage hydrogenation behind one section thermal separation condenser, and isolated gas phase is sent to two sections circulating hydrogen compressor suction tanks; Liquid phase part returns the one-stage hydrogenation hot knock-out pot, the liquid part of one-stage hydrogenation hot knock-out pot bottom is through the one-stage hydrogenation recycle pump, deliver to one section back raw pyrolysis gasoline of sending here with the one-stage hydrogenation fresh feed pump of recirculation cooler cooling and be mixed into the one-stage hydrogenation reactor head, another part enters decarburization five towers middle part;
B) decarburization five Tower Systems
Decarburization five top of tower gas phases enter decarburization five tower return tanks behind decarburization five column overhead condensers, decarburization five tower return tank dischargings are returned decarburization five tops of tower through decarburization five tower reflux pump parts, and another part is sent to carbon five product storage tanks; Decarburization five Tata still dischargings enter decarburization nine towers middle part;
Decarburization five towers are provided with decarburization five Tata still reboilers;
C) decarburization nine Tower Systems
Decarburization nine top of tower gas phases enter decarburization nine tower return tanks behind decarburization nine column overhead condensers, decarburization nine tower return tank discharging parts are returned decarburization nine tops of tower through decarburization nine tower reflux pumps, and another part is delivered to two sections input and output material interchanger through the secondary hydrogenation fresh feed pump;
Decarburization nine Tata still dischargings send carbon nine product storage tanks after the cooling of carbon nine tower reactor product coolers through decarburization nine Tata still pumps again;
D) secondary hydrogenation system
After the recycle hydrogen of material from the secondary hydrogenation fresh feed pump with two sections circulating hydrogen compressors mixes, after two sections input and output material interchanger and the heating of two section feeding process furnace, enter the secondary hydrogenation reactor head successively; The second stage reactor bottom discharge through two sections input and output material interchanger, two sections aftercoolers, is delivered to the secondary hydrogenation separating tank successively, and the isolated gas phase of secondary hydrogenation separating tank is sent two sections circulating hydrogen compressor suction tanks; Two sections circulating hydrogen compressor suction tank gas phases are sent two sections input and output material heat exchanger entrances after two sections circulating hydrogen compressors boost, the secondary hydrogenation separating tank is isolated liquid phase and entered stabilizer tower input and output material interchanger;
E) stabilizer tower system
The liquid phase of secondary hydrogenation separating tank enters the stabilizer tower middle part through the heating of stabilizer tower input and output material interchanger; Stabilizer tower cat head gas phase enters the stabilizer tower return tank through the stabilizer tower overhead condenser, and stabilizer tower return tank gas phase is sent the low-pressure tail gas pipe network, and liquid phase is returned the stabilizer tower cat head through the pressurization of stabilizer tower reflux pump; The discharging of stabilizer tower tower reactor is boosted through the hydrogenated gasoline product pump, after decarburization nine tower intermediate reboilers, stabilizer tower input and output material interchanger and the cooling of hydrogenated gasoline reactor product cooler, send hydrogenated gasoline product storage tank successively.
8. as the pyrolysis gasoline hydrogenation of total effluent device of method of hydrotreating as described in one of claim 1～7, comprise a) one-stage hydrogenation reactor (R-750) system, b) decarburization five towers (C-710) system, c) decarburization nine towers (C-720) system, d) secondary hydrogenation reactor (R-760) system, e) stabilizer tower (C-770) system; It is characterized in that:
Described decarburization nine towers (C-720) system also arranges decarburization nine tower intermediate reboilers (E-726) on decarburization nine towers (C-720) stripping section top except decarburization nine Tata still reboilers (E-725) are set;
The thermal medium entrance of described decarburization nine tower intermediate reboilers (E-726) is connected with hydrogenated gasoline product pump (P-775) outlet;
The thermal medium outlet of described decarburization nine tower intermediate reboilers (E-726) is connected with the import of stabilizer tower input and output material interchanger (E-776) thermal medium.
9. the device of pyrolysis gasoline hydrogenation of total effluent method as claimed in claim 8 is characterized in that:
Described device comprises following equipment successively:
A) one-stage hydrogenation reactor (R-750) system
The raw pyrolysis gasoline raw material connects following equipment by raw pyrolysis gasoline storage tank (TK-700) successively through pipeline: raw gasline charging strainer (SR-700), a section feeding surge tank (D-750), one-stage hydrogenation fresh feed pump (P-750), and one-stage hydrogenation fresh feed pump (P-750) outlet is connected to one-stage hydrogenation reactor (R-750) top through pipeline;
Hydrogen is connected to one-stage hydrogenation reactor (R-750) top through pipeline by the hydrogen pipe network;
One-stage hydrogenation reactor (R-750) outlet at bottom connects one-stage hydrogenation hot knock-out pot (D-751) through pipeline, and wherein: one-stage hydrogenation hot knock-out pot (D-751) tank deck gaseous phase outlet connects one section thermal separation condenser (E-752) and the cold separating tank of one-stage hydrogenation (D-752) successively through pipeline; One-stage hydrogenation hot knock-out pot (D-751) jar end liquid phase outlet connects one-stage hydrogenation recycle pump (P-751) entrance and decarburization five towers (C-710) middle part opening for feed respectively through pipeline; One-stage hydrogenation recycle pump (P-751) outlet is connected to one section recirculation cooler (E-751) thermal medium entrance through pipeline; The outlet of one section recirculation cooler (E-751) thermal medium is connected to one-stage hydrogenation reactor (R-750) top through pipeline;
The cold separating tank of one-stage hydrogenation (D-752) top gaseous phase outlet connects two sections circulating hydrogen compressor suction tanks (D-761) through pipeline; The cold separating tank of one-stage hydrogenation (D-752) jar end liquid phase outlet connects one-stage hydrogenation hot knock-out pot (D-751) through pipeline;
B) decarburization five towers (C-710) system
Decarburization five towers (C-710) cat head gaseous phase outlet connects following equipment successively through pipeline: decarburization five column overhead condensers (E-710), decarburization five tower return tanks (D-710), decarburization five tower reflux pumps (P-715);
The outlet of decarburization five tower reflux pumps (P-715) connects respectively through pipeline: decarburization five towers (C-710) top refluxing opening, carbon five product storage tank (TK-710) opening for feeds;
The outlet of decarburization five towers (C-710) tower reactor liquid phase connects decarburization nine towers (C-720) middle part opening for feed through pipeline;
Decarburization five towers (C-710) tower reactor reboiler extraction mouth is connected to the cold medium import of decarburization five Tata still reboilers (E-715) through pipeline, and the cold media outlet of decarburization five Tata still reboilers (E-715) is connected to decarburization five towers (C-710) tower reactor reboiler return port through pipeline;
C) decarburization nine towers (C-720) system
Decarburization nine towers (C-720) cat head gaseous phase outlet connects following equipment successively through pipeline: decarburization nine column overhead condensers (E-720), decarburization nine tower return tanks (D-720);
Jar end liquid phase outlet of decarburization nine tower return tanks (D-720) connects decarburization nine tower reflux pump (P-720) entrances and secondary hydrogenation fresh feed pump (P-721) entrance respectively through pipeline; The outlet of decarburization nine tower reflux pumps (P-720) connects decarburization nine towers (C-720) top refluxing opening through pipeline; Secondary hydrogenation fresh feed pump (P-721) outlet is connected to the cold medium import of two sections input and output material interchanger (E-760) through pipeline;
Decarburization nine tower return tank (D-720) tank deck gas phase pipelines connect decarburization nine tower tail gas condenser (E-721) thermal medium imports; The outlet of decarburization nine tower tail gas condenser (E-721) thermal medium liquid phases connects decarburization nine tower return tanks (D-720) through pipeline, and decarburization nine tower tail gas condenser (E-721) thermal medium gaseous phase outlets connect the entrance of decarburization nine tower vacuum systems (PA-720) through pipeline; The outlet of decarburization nine tower vacuum systems (PA-720) is connected to vacuum tail gas pipe network through pipeline;
Decarburization nine towers (C-720) tower reactor connects following equipment successively through pipeline: decarburization nine Tata still pumps (P-725), carbon nine reactor product coolers (E-728), carbon nine product storage tanks (TK-720);
Decarburization nine towers (C-720) tower reactor reboiler extraction mouth is connected to the cold medium import of decarburization nine Tata still reboilers (E-725) through pipeline, and the cold media outlet of decarburization nine Tata still reboilers (E-725) is connected to decarburization nine towers (C-720) tower reactor reboiler return port through pipeline;
Decarburization nine towers (C-720) intermediate reboiler extraction mouth is connected to the cold medium import of decarburization nine tower intermediate reboilers (E-726) through pipeline, and the cold media outlet of decarburization nine tower intermediate reboilers (E-726) is connected to decarburization nine towers (C-720) intermediate reboiler return port through pipeline;
D) secondary hydrogenation reactor (R-760) system
The cold media outlet of two sections input and output material interchanger (E-760) is connected to the cold medium import of two section feeding process furnace (F-760) through pipeline, and the cold medium import of two section feeding process furnace (F-760) is connected to secondary hydrogenation reactor (R-760) top inlet through pipeline;
Secondary hydrogenation reactor (R-760) outlet at bottom is connected to two sections input and output material interchanger (E-760) thermal medium entrance through pipeline; The outlet of two sections input and output material interchanger (E-760) thermal medium is connected to two sections aftercondensers (E-761) thermal medium entrance respectively through pipeline; The outlet of two sections aftercondensers (E-761) thermal medium is connected to secondary hydrogenation separating tank (D-760) import;
The gaseous phase outlet at secondary hydrogenation separating tank (D-760) top is connected to two sections circulating hydrogen compressor suction tanks (D-761) through pipeline; Two sections circulating hydrogen compressor suction tanks (D-761) top gaseous phase outlet is connected to two sections circulating hydrogen compressors (K-760) entrance through pipeline; Two sections circulating hydrogen compressors (K-760) outlets is connected to connection line between secondary hydrogenation fresh feed pump (P-721) and two sections input and output material interchanger (E-760) through pipeline;
The outlet of secondary hydrogenation separating tank (D-760) bottom liquid phases is connected to the cold medium import of stabilizer tower input and output material interchanger (E-776) through pipeline;
E) stabilizer tower (C770) system
The cold media outlet of stabilizer tower input and output material interchanger (E-776) is connected to stabilizer tower (C-770) middle part opening for feed through pipeline;
Stabilizer tower (C-770) overhead line connects successively: stabilizer tower overhead condenser (E-770), stabilizer tower return tank (D-770); Stabilizer tower return tank (D-770) jar end liquid phase outlet is connected to stabilizer tower reflux pump (P-770) entrance through pipeline; Stabilizer tower reflux pump (P-770) outlet is connected to stabilizer tower (C-770) trim the top of column mouth through pipeline; Stabilizer tower return tank (D-770) tank deck gaseous phase outlet is connected to the low-pressure tail gas pipe network through pipeline;
Stabilizer tower (C-770) tower reactor discharge port is connected to hydrogenated gasoline product pump (P-775) entrance through pipeline; Hydrogenated gasoline product pump (P-775) outlet is connected to decarburization nine tower intermediate reboiler (E-726) thermal medium entrances through pipeline; The outlet of decarburization nine tower intermediate reboiler (E-726) thermal mediums is connected to stabilizer tower input and output material interchanger (E-776) thermal medium entrance through pipeline; The outlet of stabilizer tower input and output material interchanger (E-776) thermal medium is connected to hydrogenated gasoline water cooler (E-777) thermal medium entrance through pipeline; The outlet of hydrogenated gasoline water cooler (E-777) thermal medium is connected to hydrogenated gasoline product storage tank (TK-770) through pipeline;
Stabilizer tower (C-770) tower reactor reboiler extraction mouth is connected to the cold medium import of stabilizer tower tower reactor reboiler (E-775) through pipeline, and the cold media outlet of stabilizer tower tower reactor reboiler (E-775) is connected to stabilizer tower (C-770) tower reactor reboiler return port through pipeline.
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| CN103657264B (en) * | 2012-09-25 | 2016-09-14 | 中国石油化工股份有限公司 | Remove recycle hydrogen drop and the devices and methods therefor of granule in hydrogenated pyrolysis gasoline |
| CN103982739B (en) * | 2014-04-11 | 2016-08-17 | 中国石油化工股份有限公司青岛安全工程研究院 | The pre-thermal flow process of high temperature oil pulp grinder pump |
| CN105087065B (en) * | 2014-05-15 | 2017-01-25 | 中国石化工程建设有限公司 | Pyrolysis gasoline central fraction hydrogenation device and method thereof |
| CN105647581B (en) * | 2014-11-12 | 2017-09-15 | 中国石油天然气股份有限公司 | Gasoline hydrogenation method |
| CN104593064B (en) * | 2015-02-05 | 2016-02-24 | 中石化上海工程有限公司 | The separation method of pyrolysis gasoline hydrogenation device second stage reactor outlet material |
| CN104560161A (en) * | 2015-02-05 | 2015-04-29 | 中石化上海工程有限公司 | Method for heating materials at inlet of second-stage reactor of pyrolysis gasoline hydrogenation device |
| CN106281448B (en) * | 2016-09-23 | 2018-09-07 | 北京石油化工工程有限公司 | The optimum organization production method and system of a kind of aromatic hydrocarbons, alkane and solvent naphtha |
| CN107325840B (en) * | 2017-06-02 | 2019-02-19 | 北京启迪安圆能源环境工程技术有限公司 | A kind of drippolene C9+The hydrotreater and technique of fraction |
| CN115948180B (en) * | 2023-03-14 | 2023-05-23 | 新疆天利石化股份有限公司 | Energy-saving and environment-friendly process for producing mixed aromatic hydrocarbon by cracking carbon nine and hydrogenation |
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