CN208791574U - A kind of pyrolysis gasoline hydrogenation system using high-performance heat exchanger - Google Patents
A kind of pyrolysis gasoline hydrogenation system using high-performance heat exchanger Download PDFInfo
- Publication number
- CN208791574U CN208791574U CN201821360637.1U CN201821360637U CN208791574U CN 208791574 U CN208791574 U CN 208791574U CN 201821360637 U CN201821360637 U CN 201821360637U CN 208791574 U CN208791574 U CN 208791574U
- Authority
- CN
- China
- Prior art keywords
- sections
- section
- entrance
- hydrogenation
- outlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
This disclosure relates to which a kind of pyrolysis gasoline hydrogenation system using high-performance heat exchanger, including one-stage hydrogenation consersion unit and secondary hydrogenation consersion unit, one-stage hydrogenation consersion unit extend one-stage hydrogenation discharge port, secondary hydrogenation consersion unit includes second-stage hydrogenation reactor；There is secondary hydrogenation feed heating device, secondary hydrogenation feed heating device is made of two sections of input and output material heat exchangers, and the thermal medium entrance of two sections of input and output material heat exchangers is connected to the discharge port of second-stage hydrogenation reactor between one-stage hydrogenation discharge port and second-stage hydrogenation reactor；Or, secondary hydrogenation feed heating device is made of two section feeding preheaters and two sections of input and output material heat exchangers, the thermal medium entrance of two sections of input and output material heat exchangers is connected to the discharge port of second-stage hydrogenation reactor, and the thermal medium entrance of two section feeding preheaters is connected to the liquid-phase outlet of subsequent stabilizer；Two sections of input and output material heat exchangers are high-performance heat exchanger.The system can make full use of hydrogenation reaction hot, make secondary hydrogenation without additional additional heat, reduce system energy consumption.
Description
Technical field
This disclosure relates to a kind of pyrolysis gasoline hydrogenation system using high-performance heat exchanger.
Background technique
Currently, industrial pyrolysis gasoline hydrogenation is typically all that the method for using two-stage catalytic selective hydrogenation removes cracking vapour
The a large amount of unsaturates and impurity contained in oil, such as monoolefine, alkadienes, alkenyl arene, sulfide.Wherein, first segment adds
Hydrogen is to carry out liquid phase reactor under the conditions of relatively mitigating, and hydrogen purpose is added mainly to make di-olefins monoolefine, alkenyl arene
It is converted into alkylaromatic hydrocarbon；Second segment adds hydrogen to be at relatively high temperatures, to carry out gas phase reaction, and hydrogen purpose is added mainly to make monoolefine
It is converted into saturated hydrocarbons, sulfide is converted into H2S。
According to chemical principle, hydrogenation of unsaturated hydrocarbons is exothermic reaction, and existing procedure is arranged in second-stage reaction system
Second stage reactor feeding temperature can not be heated to the temperature that reaction requires to recycle heat by input and output material heat exchanger, therefore,
Current existing pyrolysis gasoline hydrogenation device is provided with the heating equipments such as heating furnace or electric heater in second stage reactor entrance.
Heating furnace is energy consumption rich and influential family, while being also one of the main source of flue gas emission.The fuel source of heating furnace
The mainly non-renewable fossil energy such as fuel oil, fuel gas removes CO by the flue gas that burning generates2、H2O and N2Except, together
When also with NOXAnd SOXGeneration.Requirement with country to environmental protection increasingly becomes sternly, and the presence of some areas heating furnace has become
Problem.And many newly-built pyrolysis gasoline hydrogenation devices are to agree with national requirements for environmental protection, have replaced heating furnace with electric heater, but
Consequent is higher operating cost.
Utility model content
Purpose of this disclosure is to provide a kind of pyrolysis gasoline hydrogenation system, the secondary hydrogenation reaction system of the system can be returned
More reaction heat are received, without introducing external heat source.
To achieve the goals above, the disclosure provides a kind of pyrolysis gasoline hydrogenation system, which includes that one-stage hydrogenation is anti-
Equipment and secondary hydrogenation consersion unit are answered, the one-stage hydrogenation consersion unit extends one-stage hydrogenation discharge port, and described two sections add
Hydrogen consersion unit includes second-stage hydrogenation reactor；Have two between the one-stage hydrogenation discharge port and the second-stage hydrogenation reactor
Section plus hydrogen feed heating device, the secondary hydrogenation feed heating device is made of two sections of input and output material heat exchangers, described two sections into
The thermal medium entrance of effluent exchanger is connected to the discharge port of the second-stage hydrogenation reactor；Alternatively, the secondary hydrogenation charging
Heating device is made of two section feeding preheaters and two sections of input and output material heat exchangers, and the secondary hydrogenation consersion unit further includes stablizing
The thermal medium entrance of tower, two sections of input and output material heat exchangers is connected to the discharge port of the second-stage hydrogenation reactor, and described two sections
The thermal medium entrance of feed preheater is connected to the liquid-phase outlet of the stabilizer；Wherein, two sections of input and output material heat exchangers are
High-performance heat exchanger.
Optionally, the secondary hydrogenation feed heating device does not connect with the heat source of the pyrolysis gasoline hydrogenation exterior
It is logical.
Optionally, the high-performance heat exchanger includes that coiled heat exchanger, plate heat exchanger, finned tube exchanger, falling liquid film change
Hot device, tube with high flux heat exchanger, spiral baffle heat exchanger or distortion heat exchange of heat pipe.
Optionally, the pyrolysis gasoline hydrogenation system further includes hydrogen inlet, feed(raw material)inlet, two sections of separators and product
Outlet, the hydrogen inlet and the feed(raw material)inlet are connected to the one-stage hydrogenation consersion unit respectively, two sections of input and output materials
The thermal medium outlet of heat exchanger is connected to the entrance of two sections of separators；The one-stage hydrogenation discharge port with described two sections into
The cold medium entrance of effluent exchanger is connected to, and the cold medium outlet of two sections of input and output material heat exchangers is reacted with the secondary hydrogenation
The entrance of device is connected to, and the liquid-phase outlet of two sections of separators is connected to the product exit of the pyrolysis gasoline hydrogenation system；
Alternatively, the one-stage hydrogenation discharge port is connected to the cold medium entrance of the two section feedings preheater, the two section feedings preheating
Device cold medium outlet be connected to the cold medium entrance of two sections of input and output material heat exchangers, two sections of input and output material heat exchangers it is cold
Media outlet is connected to the entrance of the second-stage hydrogenation reactor, the liquid-phase outlet and the stabilizer of two sections of separators
Entrance connection, the product exit of the thermal medium outlet of the two section feedings preheater and the pyrolysis gasoline hydrogenation system connects
It is logical.
Optionally, two sections of separators include two sections of heat separators, secondary hydrogenation aftercooler and two sections of cold separators；
The entrance of two sections of separators is connected to the entrance of two sections of heat separators, the liquid-phase outlet of two sections of heat separators
Be connected to the liquid-phase outlet of two sections of separators, the gaseous phase outlet of two sections of heat separators with it is cold after the secondary hydrogenation
The thermal medium entrance of device is connected to, and the entrance of the thermal medium outlet of the secondary hydrogenation aftercooler and two sections of cold separators connects
Logical, the gaseous phase outlet of two sections of cold separators is connected to the gaseous phase outlet of two sections of separators, two sections of cold separation
The liquid-phase outlet of device is connected to the entrance of two sections of heat separators.
Optionally, the secondary hydrogenation reaction system further includes compressor suction tank and circulating hydrogen compressor, and described two sections
The gaseous phase outlet of separator is connected to the entrance of the compressor suction tank, and the outlet of the compressor suction tank is followed with described
The entrance of ring hydrogen compressor is connected to, and the outlet of the circulating hydrogen compressor is connected to the one-stage hydrogenation discharge port.
Optionally, the one-stage hydrogenation reaction system includes feed surge tank, feed pump, one-stage hydrogenation reactor and one section
Separator；The one-stage hydrogenation reactor has gas access and liquid inlet, the hydrogen inlet of the system and described one
The gas access connection of section hydrogenator, the feed(raw material)inlet of described device is connected to the entrance of the feed surge tank, described
The outlet of feed surge tank is connected to the entrance of the feed pump, outlet and the one-stage hydrogenation reactor of the feed pump
Liquid inlet connection；The outlet of the one-stage hydrogenation reactor is connected to the entrance of one section of separator, and described one section point
There is gaseous phase outlet and liquid-phase outlet from device, the liquid-phase outlet and the one-stage hydrogenation discharge port of one section of separator connect
It is logical.
Optionally, one section of separator includes one section of heat separator, one section of thermal release condenser and one section of cold separation
Device；The entrance of one section of separator is connected to the entrance of one section of heat separator, the gas phase of one section of heat separator
Outlet is connected to the thermal medium entrance of one section of thermal release condenser, the liquid-phase outlet and described one of one section of heat separator
The liquid-phase outlet connection of section separator；The thermal medium outlet of one section of thermal release condenser and one section of cold separator
Entrance connection, the gaseous phase outlet of one section of cold separator are connected to the gaseous phase outlet of one section of separator, and described one section
The liquid-phase outlet of cold separator is connected to the entrance of one section of heat separator.
Optionally, which further includes dispensing pump and one section of recirculation cooler, the entrance of the dispensing pump with described one section
The liquid-phase outlet of separator is connected to, and the first outlet of the dispensing pump is connected to the one-stage hydrogenation discharge port, the distribution
The second outlet of pump is connected to the entrance of one section of recirculation cooler, the outlet of one section of recirculation cooler with described one section
The liquid inlet of hydrogenator is connected to.
Optionally, which further includes regenerator, and the regeneration gas outlet of the regenerator is successively anti-with the secondary hydrogenation
Device is answered to be connected to two sections of input and output material heat exchangers.
Through the above technical solutions, the pyrolysis gasoline hydrogenation system of the disclosure is in secondary hydrogenation equipment by using efficiently changing
Hot device can recycle more reaction heat, the heat for making full use of secondary hydrogenation reaction to release for charging heating, so that secondary hydrogenation
Equipment no longer needs additional additional heat, improves the recovery utilization rate of heat, reduces system energy consumption.The system of the disclosure can
It realizes that two anti-equipment heats are self-sufficient, avoids disposably solving energy consumption and environmentally friendly two hang-ups using heating furnace.
Other feature and advantage of the disclosure will the following detailed description will be given in the detailed implementation section.
Detailed description of the invention
Attached drawing is and to constitute part of specification for providing further understanding of the disclosure, with following tool
Body embodiment is used to explain the disclosure together, but does not constitute the limitation to the disclosure.In the accompanying drawings:
Fig. 1 is a kind of schematic diagram of specific embodiment of the pyrolysis gasoline hydrogenation system of the disclosure.
Fig. 2 is the schematic diagram of the pyrolysis gasoline hydrogenation system of the comparative example (prior art) of the disclosure.
Description of symbols
1 feed(raw material)inlet, 2 hydrogen inlet
The liquid-phase outlet of 34 two sections of separators of product exit
The liquid-phase outlet of 6 stabilizer of gaseous phase outlet of 5 two sections of separators
Mono- mono- section of heat separator of section feeding surge tank D-751 of D-750
Mono- section of D-752 cold separator D-760, bis- sections of heat separators
D-761 compressor suction tank bis- sections of cold separators of D-762
Mono- section of E-751, mono- section of recirculation cooler E-752 thermal release condenser
Bis- sections of bis- section feeding preheaters of input and output material heat exchanger E-762 of E-760
Bis- section feeding heating furnace of E-763 secondary hydrogenation aftercooler F-760
K-760 circulating hydrogen compressor P-750 feed pump
P-751 dispensing pump R-750 one-stage hydrogenation reactor
Bis- sections of input and output material heat exchangers of R-760 second-stage hydrogenation reactor E-765
Specific embodiment
It is described in detail below in conjunction with specific embodiment of the attached drawing to the disclosure.It should be understood that this place is retouched
The specific embodiment stated is only used for describing and explaining the disclosure, is not limited to the disclosure.
In the disclosure, in the absence of explanation to the contrary, the noun of locality used such as " upper and lower " typically refers to device and exists
It is upper and lower under normal operating condition, specifically it is referred to the page of Fig. 1." inside and outside " is the profile for device itself
For.
As shown in Figure 1, the disclosure provides a kind of pyrolysis gasoline hydrogenation system, the system include one-stage hydrogenation consersion unit and
Secondary hydrogenation consersion unit, one-stage hydrogenation consersion unit extend one-stage hydrogenation discharge port, and secondary hydrogenation consersion unit includes two
Section hydrogenator R-760；There is secondary hydrogenation charging heating between one-stage hydrogenation discharge port and second-stage hydrogenation reactor R-760
Device, secondary hydrogenation feed heating device are made of two sections of input and output material heat exchanger E-765, two sections of input and output material heat exchanger E-765's
Thermal medium entrance is connected to the discharge port of second-stage hydrogenation reactor R-760；Alternatively, secondary hydrogenation feed heating device by two sections into
Expect preheater E-762 and two sections of input and output material heat exchanger E-765 composition, secondary hydrogenation consersion unit further includes stabilizer, two sections into
The thermal medium entrance of effluent exchanger E-765 is connected to the discharge port of second-stage hydrogenation reactor R-760, two section feeding preheater E-
762 thermal medium entrance is connected to the liquid-phase outlet 6 of stabilizer；Wherein, two sections of input and output material heat exchangers are high-performance heat exchanger.
The pyrolysis gasoline hydrogenation system of the disclosure is used in secondary hydrogenation equipment using the heat exchanger with high heat exchange efficiency, energy
More reaction heat, the heat for making full use of secondary hydrogenation reaction to release enough are recycled for charging heating, so that secondary hydrogenation equipment is not
Additional additional heat is needed again, improves the recovery utilization rate of heat, to reduce plant energy consumption.
According to the disclosure, the heat source of secondary hydrogenation feed heating device from second-stage hydrogenation reactor product and can
Selection of land from stabilizer product, as a result, in the disclosure, secondary hydrogenation feed heating device not with any drippolene
Heat source connection outside hydrogenation system, specifically, secondary hydrogenation feed heating device is not connected to exterior heat source to be referred to, two
Do not include the heating equipments such as heating furnace in section hydrogenation plant, do not use yet the heat sources such as the high-temperature steam outside system to feed into
Row heating.In the embodiment that secondary hydrogenation feed heating device is made of two sections of input and output material heat exchangers, two sections of input and output materials are changed
The heat exchange efficiency of hot device is high, therefore can make full use of the heat that secondary hydrogenation reaction generates is that two anti-chargings are heated；?
In the embodiment that secondary hydrogenation feed heating device is made of two sections of input and output material heat exchangers and two section feeding preheaters, Ke Yixian
It is the feeding preheating of secondary hydrogenation using the heat in the product of stabilizer, then recycles two sections of disengaging of high efficient heat exchanging
Material heat exchanger is heated, and thus, it is possible to reduce the cooling water amount cooling for stabilizer product, is taken full advantage of in system
Heat, improve energy utilization efficiency, and saved system energy consumption.
According to the disclosure, what the meaning of high-performance heat exchanger was well known to those skilled in the art, i.e., it is situated between in identical heat exchange
Under the conditions of matter, the heat exchange efficiency of high-performance heat exchanger is higher, and more compact structure, and identical heat exchange area the space occupied is smaller.
High-performance heat exchanger can be changed selected from coiled heat exchanger, plate heat exchanger, finned tube exchanger, Falling film heat transfer device, tube with high flux
Hot device, spiral baffle heat exchanger, distortion heat exchange of heat pipe etc. have at least one of heat exchanger pattern of augmentation of heat transfer function,
What the high-performance heat exchanger of mentioned kind was well known to those skilled in the art, it is not repeated herein.Further, in order to improve two
The heat exchange efficiency of section input and output material heat exchanger, two sections of input and output material heat exchanger E-765 are preferably coiled heat exchanger, and model is without spy
It is different to require, it can be commercially available.Coiled heat exchanger (also known as wrap-round tubular heat exchanger) can be this field conventional kind,
Heat-transfer pipe is replaced by helix shape in space i.e. between core cylinder and outer cylinder and is entwined, the heat transfer of adjacent two layers helical form
The hand of spiral of pipe using the distance pieces of certain shapes on the contrary, and be allowed to keep the high-performance heat exchanger of certain spacing, the disclosure
Used coiled heat exchanger is, for example, sub-thread stream wrap-round tubular heat exchanger or multiple flow wrap-round tubular heat exchanger.
According to the disclosure, as shown in Figure 1, pyrolysis gasoline hydrogenation system can also include hydrogen inlet 2, feed(raw material)inlet 1, two
Section separator and product exit 3, hydrogen inlet 2 and feed(raw material)inlet 1 can be connected to one-stage hydrogenation consersion unit respectively.
Wherein, the reality being made of in secondary hydrogenation feed heating device two sections of input and output material heat exchangers and two section feeding preheaters
It applies in mode, one-stage hydrogenation discharge port can be connected to the cold medium entrance of two sections of input and output material heat exchanger E-765, two sections of input and output materials
The cold medium outlet of heat exchanger E-765 can be connected to the entrance of second-stage hydrogenation reactor R-760, two sections of input and output material heat exchanger E-
765 thermal medium outlet can be connected to the entrance of two sections of separators, and the liquid phase 4 of two sections of separators can be with drippolene
The product exit 3 of hydrogenation system is connected to.
In order to further separate the hydrogen sulfide in hydrogenation products, changed in secondary hydrogenation feed heating device by two sections of input and output materials
In the embodiment of hot device and two section feeding preheaters composition, as shown in Figure 1, one-stage hydrogenation discharge port can be pre- with two section feedings
The cold medium entrance of hot device E-762 is connected to, and the cold medium outlet of two section feeding preheater E-762 can exchange heat with two sections of input and output materials
The cold medium entrance of device E-765 is connected to, and the cold medium outlet of two sections of input and output material heat exchanger E-765 can be with second-stage hydrogenation reactor
The entrance of R-760 is connected to, and the thermal medium outlet of two sections of input and output material heat exchanger E-765 can connect with the entrance of two sections of separators
Logical, the liquid-phase outlet 4 of two sections of separators can be connected to the entrance of stabilizer, the thermal medium of two section feeding preheater E-762
Outlet can be connected to the product exit 3 of pyrolysis gasoline hydrogenation system.
According to the disclosure, two sections of separators can be used for separating secondary hydrogenation reaction product, the packet of two sections of separators
The separator type and connection type contained can be this field routine.It is excellent in the disclosure in order to further increase separative efficiency
Choosing a kind of specific embodiment in, as shown in Figure 1, two sections of separators may include two sections of heat separator D-760, two sections plus
Hydrogen aftercooler E-763 and two sections of cold separator D-762；The entrance of two sections of separators can be with two sections of heat separator D-760's
Entrance connection, the liquid-phase outlet of two sections of heat separator D-760 can be connected to the liquid-phase outlet 4 of two sections of separators, two sections of heat
The gaseous phase outlet of separator D-760 can be connected to the thermal medium entrance of secondary hydrogenation aftercooler E-763, secondary hydrogenation aftercooler
The thermal medium outlet of E-763 can be connected to the entrance of two sections of cold separator D-762, and the gas phase of two sections of cold separator D-762 goes out
Mouth can be connected to the gaseous phase outlet 5 of two sections of separators, and the liquid-phase outlet of two sections of cold separator D-762 can be with two sections of warm point
Entrance connection from device D-760.
Further, for the ease of recycling the hydrogen in the light component that two sections of separators are isolated, in the disclosure
A kind of specific embodiment in, secondary hydrogenation reaction system can also include compressor suction tank D-761 and circulation hydrogen compressed
The gaseous phase outlet of machine K-760, two sections of separators can be connected to the entrance of compressor suction tank D-761, compressor suction tank
The outlet of D-761 can be connected to the entrance of circulating hydrogen compressor K-760, and the outlet of circulating hydrogen compressor K-760 can be with one
Section plus the connection of hydrogen discharge port.
In a kind of specific embodiment of the disclosure, as shown in Figure 1, one-stage hydrogenation reaction system may include one section into
Surge tank D-750, feed pump P-750, one-stage hydrogenation reactor R-750 and one section of separator are expected, in order to smoothly carry out
One-stage hydrogenation reaction；One-stage hydrogenation reactor R-750 has gas access and a liquid inlet, and the hydrogen inlet 2 of system can be with
The gas access of one-stage hydrogenation reactor R-750 is connected to, and the feed(raw material)inlet 1 of device can be with a section feeding surge tank D-750's
Entrance connection, the outlet of a section feeding surge tank D-750 can be connected to the entrance of feed pump P-750, and feed pump P-750's goes out
Mouth can be connected to the liquid inlet of one-stage hydrogenation reactor R-750；It the outlet of one-stage hydrogenation reactor R-750 can be with one section
The entrance of separator is connected to, and is separated with the product to one-stage hydrogenation reactor R-750, and one section of separator has gas phase
Outlet and liquid-phase outlet, the liquid-phase outlet of one section of separator can be connected to one-stage hydrogenation discharge port, to add hydrogen for first
Product send to secondary hydrogenation equipment and carries out secondary hydrogenation.
According to the disclosure, one section of separator can be used for separating the product of one-stage hydrogenation reaction, one section of separator packet
The separator type and connection type contained can be this field routine.It is excellent in the disclosure in order to further increase separative efficiency
In a kind of specific embodiment of choosing, as shown in Figure 1, one section of separator may include one section of heat separator D-751, one section of heat
Separation condenser E-752 and one section of cold separator D-752；The entrance of one section of separator can be with one section of heat separator D-751
Entrance connection, the gaseous phase outlet of one section of heat separator D-751 can be with the thermal medium entrance of one section of thermal release condenser E-752
Connection, the liquid-phase outlet of one section of heat separator D-751 can be connected to the liquid-phase outlet of one section of separator；One section of thermal release is cold
The thermal medium outlet of condenser E-752 can be connected to the entrance of one section of cold separator D-752, the gas of one section of cold separator D-752
Mutually outlet can be connected to the gaseous phase outlet of one section of separator, and the liquid-phase outlet of one section of cold separator D-752 can be with one section
The entrance of heat separator D-751 is connected to.
It further, further include compressor suction tank D-761 and circulating hydrogen compressor K-760 in secondary hydrogenation reaction system
Embodiment in, the gaseous phase outlet of one section of separator can also be connected to the entrance of compressor suction tank D-761, i.e., one section
The gaseous phase outlet of cold separator D-752 can be connected to the entrance of compressor suction tank D-761.
For regulating system temperature, in a kind of specific embodiment of the disclosure, which can also include dispensing pump
The entrance of P-751 and one section of recirculation cooler E-751, dispensing pump P-751 can be connected to the liquid-phase outlet of one section of separator,
The first outlet of dispensing pump P-751 can be connected to one-stage hydrogenation discharge port, and the second outlet of dispensing pump P-751 can be with one section
The entrance of recirculation cooler E-751 is connected to, and the outlet of one section of recirculation cooler E-751 can be with one-stage hydrogenation reactor R-750
Liquid inlet connection, to enter the flow of secondary hydrogenation equipment by dispensing pump P-751 adjusting one-stage hydrogenation product.
In a kind of specific embodiment of the disclosure, which can also include regenerator, react for secondary hydrogenation
The regeneration of device and two sections of input and output material heat exchangers influences hydrogenation reaction with slagging prevention and carries out, and the regeneration gas outlet of regenerator is preferred
It is successively connected to second-stage hydrogenation reactor R-760 and two sections of input and output material heat exchanger E-765, so that regeneration gas first passes through secondary hydrogenation
Reactor R-760 passes through the tube side and shell side of two sections of input and output material heat exchanger E-765 again, to complete regenerative process.
The disclosure is explained further by the following examples, but therefore the disclosure is not any way limited.
Comparative example
The pyrolysis gasoline hydrogenation system of this comparative example is as shown in Figure 2.Upstream C6~C8 hydrocarbon enters a section feeding as raw material
Surge tank D-750, D-750 outlet at bottom is connected to feed pump P-750 entrance through pipeline；The outlet feed pump P-750 connects through pipeline
The connecting pipeline being connected between one section of recirculation cooler E-751 thermal medium outlet and one-stage hydrogenation reactor R-750；
Hydrogen gas lines are connected at the top of one-stage hydrogenation reactor R-750 by hydrogen pipe network through pipeline；
One-stage hydrogenation reactor R-750 outlet at bottom connects one section of heat separator D-751 through pipeline；One section of heat separator D-
751 tank deck gaseous phase outlets are connected to one section of thermal release condenser E-752 thermal medium entrance, one section of thermal release condenser E- through pipeline
752 thermal medium outlets are connected to one section of cold separator D-752 entrance through pipeline；One section of heat separator D-751 tank bottom liquid-phase outlet
Dispensing pump P-751 entrance is connected through pipeline；The outlet dispensing pump P-751 is separately connected one section of recirculation cooler E-751 heat through pipeline
Medium inlet and two section feeding preheater E-762 cold medium imports；One section of recirculation cooler E-751 thermal medium outlet connects through pipeline
It is connected to the top one-stage hydrogenation reactor R-750；
One section of cold separator D-752 top gas phase outlet is connected to compressor suction tank D-761 through pipeline；One section of cold separation
Device D-752 tank bottom liquid-phase outlet connects one section of heat separator D-751 through pipeline；
Dispensing pump P-751 exit portion material enters two anti-systems, and two section feeding preheater E-762 cold mediums are exported through pipe
Line is connected to two sections of input and output material heat exchanger E-760 cold medium entrances, and two sections of input and output material heat exchanger E-760 cold medium outlets are through pipeline
Two section feeding heating furnace F-760 cold medium imports are connected to, the outlet of two section feeding heating furnace F-760 cold mediums is connected to through pipeline
Second-stage hydrogenation reactor R-760 top inlet；
Second-stage hydrogenation reactor R-760 outlet at bottom is connected to two sections of input and output material heat exchanger E-760 thermal mediums through pipeline and enters
Mouthful；Two sections of input and output material heat exchanger E-760 thermal medium outlets are connected to two sections of heat separator D-760 imports through pipeline；
Gaseous phase outlet at the top of two sections of heat separator D-760 enters through pipeline connection secondary hydrogenation aftercooler E-763 thermal medium
Mouthful；Secondary hydrogenation aftercooler E-763 thermal medium outlet is connected to two sections of cold separator D-762 through pipeline；Two sections of cold separator D-
The gaseous phase outlet at 762 tops is connected to compressor suction tank D-761 through pipeline；The outlet of compressor suction tank D-761 top gas phase
Circulating hydrogen compressor K-760 entrance is connected to through pipeline；The outlet circulating hydrogen compressor K-760 is connected to dispensing pump P- through pipeline
751 and two connecting pipelines between section feeding preheater E-762；
Two sections of heat separator D-760 bottom liquid phases outlets are connected to the entrance of stabilizer (not shown) through pipeline.
Embodiment
Using the system of comparative example 1, the difference is that the input and output material using coiled heat exchanger as second-stage reaction system
Heat exchanger, as shown in Figure 1, being not provided with two section feeding heating furnace F-760.Two section feeding preheater E-762 cold mediums are exported through pipe
Line is connected to two sections of input and output material heat exchanger E-765 cold medium entrances, and two sections of input and output material heat exchanger E-765 cold medium outlets are through pipeline
It is connected to second-stage hydrogenation reactor R-760 top inlet；Second-stage hydrogenation reactor R-760 outlet at bottom is connected to two sections through pipeline
Input and output material heat exchanger E-765 thermal medium entrance；Two sections of input and output material heat exchanger E-765 thermal medium outlets are connected to two sections of heat through pipeline
Separator D-760 import.The system of the present embodiment realizes the self-centered purpose of second-stage reaction equipment heat, outer without supplement
Portion's heat source.
By embodiment and comparative example it is found that the system of the disclosure can be realized the self-sufficiency of secondary hydrogenation consersion unit heat certainly
Foot, without using the heat source of exterior, has saved operating cost, and be good for the environment without using heating furnace.
The preferred embodiment of the disclosure is described in detail in conjunction with attached drawing above, still, the disclosure is not limited to above-mentioned reality
The detail in mode is applied, in the range of the technology design of the disclosure, a variety of letters can be carried out to the technical solution of the disclosure
Monotropic type, these simple variants belong to the protection scope of the disclosure.
It is further to note that specific technical features described in the above specific embodiments, in not lance
In the case where shield, it can be combined in any appropriate way.In order to avoid unnecessary repetition, the disclosure to it is various can
No further explanation will be given for the combination of energy.
In addition, any combination can also be carried out between a variety of different embodiments of the disclosure, as long as it is without prejudice to originally
Disclosed thought equally should be considered as disclosure disclosure of that.
Claims (10)
1. a kind of pyrolysis gasoline hydrogenation system, which is characterized in that the system includes that one-stage hydrogenation consersion unit and secondary hydrogenation are anti-
Equipment is answered, the one-stage hydrogenation consersion unit extends one-stage hydrogenation discharge port, and the secondary hydrogenation consersion unit includes two sections
Hydrogenator (R-760)；
There is secondary hydrogenation charging heating dress between the one-stage hydrogenation discharge port and the second-stage hydrogenation reactor (R-760)
It sets, the secondary hydrogenation feed heating device is made of two sections of input and output material heat exchangers (E-765), two sections of input and output material heat exchangers
(E-765) thermal medium entrance is connected to the discharge port of the second-stage hydrogenation reactor (R-760)；
Alternatively, the secondary hydrogenation feed heating device is by two section feeding preheaters (E-762) and two sections of input and output material heat exchanger (E-
765) it forms, the secondary hydrogenation consersion unit further includes stabilizer, the thermal medium of two sections of input and output material heat exchangers (E-765)
Entrance is connected to the discharge port of the second-stage hydrogenation reactor (R-760), the thermal medium of the two section feedings preheater (E-762)
Entrance is connected to the liquid-phase outlet of the stabilizer；
Wherein, two sections of input and output material heat exchangers (E-765) are high-performance heat exchanger.
2. system according to claim 1, which is characterized in that the secondary hydrogenation feed heating device not with the cracking
The heat source of gasoline hydrogenation exterior is connected to.
3. system according to claim 1, which is characterized in that the high-performance heat exchanger includes coiled heat exchanger, board-like
Heat exchanger, finned tube exchanger, Falling film heat transfer device, tube with high flux heat exchanger, spiral baffle heat exchanger or distortion heat exchange of heat pipe.
4. system according to claim 1, which is characterized in that the pyrolysis gasoline hydrogenation system further includes hydrogen inlet
(2), feed(raw material)inlet (1), two sections of separators and product exit (3), the hydrogen inlet (2) and the feed(raw material)inlet (1) are divided
It is not connected to the one-stage hydrogenation consersion unit, the thermal medium outlet and described two of two sections of input and output material heat exchangers (E-765)
The entrance connection of section separator；
The one-stage hydrogenation discharge port is connected to the cold medium entrance of two sections of input and output material heat exchangers (E-765), and described two sections
The cold medium outlet of input and output material heat exchanger (E-765) is connected to the entrance of the second-stage hydrogenation reactor (R-760), and described two sections
The liquid-phase outlet (4) of separator is connected to the product exit (3) of the pyrolysis gasoline hydrogenation system；Alternatively,
The one-stage hydrogenation discharge port is connected to the cold medium entrance of the two section feedings preheater (E-762), described two sections into
The cold medium outlet of material preheater (E-762) is connected to the cold medium entrance of two sections of input and output material heat exchangers (E-765), described
The cold medium outlet of two sections of input and output material heat exchangers (E-765) is connected to the entrance of the second-stage hydrogenation reactor (R-760), described
The liquid-phase outlet (4) of two sections of separators is connected to the entrance of the stabilizer, the heat of the two section feedings preheater (E-762)
Media outlet is connected to the product exit (3) of the pyrolysis gasoline hydrogenation system.
5. system according to claim 4, which is characterized in that two sections of separators include two sections of heat separator (D-
760), secondary hydrogenation aftercooler (E-763) and two sections of cold separators (D-762)；The entrance of two sections of separators with it is described
The entrance connection of two sections of heat separators (D-760), the liquid-phase outlet of two sections of heat separators (D-760) are separated with described two sections
The liquid-phase outlet (4) of device is connected to, the gaseous phase outlet and the secondary hydrogenation aftercooler of two sections of heat separators (D-760)
(E-763) thermal medium entrance connection, the thermal medium outlet of the secondary hydrogenation aftercooler (E-763) cold are separated with described two sections
The entrance of device (D-762) is connected to, the gaseous phase outlet of two sections of cold separators (D-762) and the gas phase of two sections of separators
Export (5) connection, the liquid-phase outlet of two sections of cold separators (D-762) and the entrance of two sections of heat separators (D-760)
Connection.
6. system according to claim 5, which is characterized in that the secondary hydrogenation reaction system further includes compressor sucking
Tank (D-761) and circulating hydrogen compressor (K-760), the gaseous phase outlet (5) and the compressor of two sections of separators suck
The entrance of tank (D-761) is connected to, outlet and the circulating hydrogen compressor (K-760) of the compressor suction tank (D-761)
Entrance connection, the outlet of the circulating hydrogen compressor (K-760) is connected to the one-stage hydrogenation discharge port.
7. system according to claim 4, which is characterized in that the one-stage hydrogenation reaction system is buffered including a section feeding
Tank (D-750), feed pump (P-750), one-stage hydrogenation reactor (R-750) and one section of separator；
The one-stage hydrogenation reactor (R-750) has gas access and liquid inlet, the hydrogen inlet (2) of the system and institute
The gas access connection of one-stage hydrogenation reactor (R-750) is stated, the feed(raw material)inlet (1) of described device and a section feeding buffer
The entrance of tank (D-750) is connected to, the outlet of the section feeding surge tank (D-750) and the entrance of the feed pump (P-750)
Connection, the outlet of the feed pump (P-750) is connected to the liquid inlet of the one-stage hydrogenation reactor (R-750)；Described one
The outlet of section hydrogenator (R-750) is connected to the entrance of one section of separator, and one section of separator has gas
Mutually outlet and liquid-phase outlet, the liquid-phase outlet of one section of separator are connected to the one-stage hydrogenation discharge port.
8. system according to claim 7, which is characterized in that one section of separator includes one section of heat separator (D-
751), one section of thermal release condenser (E-752) and one section of cold separator (D-752)；
The entrance of one section of separator is connected to the entrance of one section of heat separator (D-751), one section of thermal release
The gaseous phase outlet of device (D-751) is connected to the thermal medium entrance of one section of thermal release condenser (E-752), one section of heat point
Liquid-phase outlet from device (D-751) is connected to the liquid-phase outlet of one section of separator；One section of thermal release condenser (E-
752) thermal medium outlet is connected to the entrance of described one section cold separator (D-752), one section of cold separator (D-752)
Gaseous phase outlet is connected to the gaseous phase outlet of one section of separator, the liquid-phase outlet of one section of cold separator (D-752) with
The entrance of one section of heat separator (D-751) is connected to.
9. system according to claim 7, which is characterized in that the system further includes dispensing pump (P-751) and a Duan Xunhuan
The entrance of cooler (E-751), the dispensing pump (P-751) is connected to the liquid-phase outlet of one section of separator, and described point
First outlet with pump (P-751) is connected to the one-stage hydrogenation discharge port, the second outlet of the dispensing pump (P-751) and institute
The entrance connection of one section of recirculation cooler (E-751) is stated, the outlet of one section of recirculation cooler (E-751) adds with described one section
The liquid inlet of hydrogen reactor (R-750) is connected to.
10. system described according to claim 1~any one of 9, which is characterized in that the system further includes regenerator, institute
State regenerator regeneration gas outlet successively with the second-stage hydrogenation reactor (R-760) and two sections of input and output material heat exchangers (E-
765) it is connected to.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821360637.1U CN208791574U (en) | 2018-08-22 | 2018-08-22 | A kind of pyrolysis gasoline hydrogenation system using high-performance heat exchanger |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821360637.1U CN208791574U (en) | 2018-08-22 | 2018-08-22 | A kind of pyrolysis gasoline hydrogenation system using high-performance heat exchanger |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN208791574U true CN208791574U (en) | 2019-04-26 |
Family
ID=66206566
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201821360637.1U Active CN208791574U (en) | 2018-08-22 | 2018-08-22 | A kind of pyrolysis gasoline hydrogenation system using high-performance heat exchanger |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN208791574U (en) |
-
2018
- 2018-08-22 CN CN201821360637.1U patent/CN208791574U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102517065A (en) | Self-heating type biomass fast pyrolysis liquefying device | |
| CN111234878A (en) | Internal heat generation forming high-temperature supercritical water gasification system and process | |
| CN113958933A (en) | Composite energy system integrating multi-energy storage and hydrocarbon fuel preparation and method | |
| CN208791574U (en) | A kind of pyrolysis gasoline hydrogenation system using high-performance heat exchanger | |
| CN103421540B (en) | Oil-gas separation process of catalytic reforming device | |
| CN203824382U (en) | Combined heat exchange system | |
| JPS59222428A (en) | Apparatus for highly efficient methanation | |
| CN202470848U (en) | Heat pipe residual heat recovering device for heating furnace | |
| CN201028489Y (en) | Boiler used for waste heat recovery in synthesis of chloroethylene | |
| CN206069360U (en) | A kind of heat exchange of energy-conserving and environment-protective and condenser system | |
| CN210141579U (en) | Heat recovery device of high-temperature reaction gas of methanol-to-propylene device | |
| CN211896825U (en) | Internal heat generation type high-temperature supercritical water gasification system | |
| CN103292305A (en) | Radial heat tube-ordinary heat exchange tube combined type waste heat recovery device for flue tail gases | |
| CN210150715U (en) | Natural gas steam reforming hydrogen production device | |
| CN208471994U (en) | Depropanization device | |
| CN104725181B (en) | Initial separation technique of gas generated by reaction for preparing propylene from oxygen-containing compounds | |
| CN202419916U (en) | Internal circulation waste heat recycling device for heat conduction oil furnace | |
| CN201245613Y (en) | Bituminous shale oil refining tail gas cyclic utilization apparatus | |
| US10272406B2 (en) | Reactor and heater configuration synergies in paraffin dehydrogenation process | |
| CN202254890U (en) | Novel carrier gas preheater | |
| CN106907928B (en) | A kind of smelting furnace system | |
| CN103925814B (en) | A kind of combined type heat-exchange system | |
| CN216093567U (en) | Novel reaction system of propane dehydrogenation device | |
| CN111826211A (en) | Method and device for fractional condensation of coal tar | |
| CN204897777U (en) | Strip cooling arrangement and have its system alkene device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |