CN209568069U - The reaction unit of naphtha - Google Patents
The reaction unit of naphtha Download PDFInfo
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- CN209568069U CN209568069U CN201821796935.5U CN201821796935U CN209568069U CN 209568069 U CN209568069 U CN 209568069U CN 201821796935 U CN201821796935 U CN 201821796935U CN 209568069 U CN209568069 U CN 209568069U
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Abstract
This application provides a kind of reaction units of naphtha.The reaction unit includes: First Heat Exchanger, for heating to naphtha；High platinum reactor, high platinum reactor are connected to First Heat Exchanger, and high platinum reactor includes reactor shell, and reactor shell has accommodating chamber, and the first catalyst is provided in accommodating chamber, and the weight content of platinum is greater than or equal to 80%；Multiple reforming reactors being sequentially connected in series, first in multiple reforming reactors being sequentially connected in series is head end reforming reactor, the last one is end reforming reactor, the outlet of the entrance of head end reforming reactor and high platinum reactor, each reforming reactor carries out the reaction such as dehydrogenation, isomerization to naphtha, the outlet of end reforming reactor is connected to the entrance of First Heat Exchanger, and the output of end reforming reactor heats naphtha.The reaction unit can reduce the temperature drop of reforming reactor, and the thermic load of heating furnace is effectively reduced, and improve the load of reaction unit.
Description
Technical field
This application involves chemical fields, in particular to a kind of reaction unit of naphtha.
Background technique
Shenhua DCL/Direct coal liquefaction project mainly produces the multiple products such as diesel oil, gasoline, aviation kerosine and liquefied gas, is country
One of 15 key projects are to be related to the great item of national energy strategy, industrial strategy and Shenhua Group self-growth strategy
Mesh is the demonstration project of a kind of advanced clean coal technology and state coal clean conversion, is to solve China's oil supply, alleviates
An important channel of the China to the dependence of imported crude oil.
The fragrant potential content of DCL/Direct coal liquefaction naphtha is higher, is 78%, generallys use fixed bed and reforms four reactor strings
The carry out dehydrogenation reaction of the technique of connection, since the thermal discharge of reaction is larger, total temperature drop of this four reactors is up to 312 DEG C,
In, the temperature drop of first reactor is 121 DEG C, and the temperature drop of second reactor is 88 DEG C, and the temperature drop of third reactor is 58 DEG C, the 4th
The temperature drop of reactor is 45 DEG C；The total temperature drop of reactor is significantly larger than conventional naphtha fixed bed and reforms 220 DEG C of numerical value, especially the
One reactor and the temperature drop of second reactor are higher, cause the thermic load of heating furnace higher, and heated material difficulty is big.
Utility model content
The main purpose of the application is to provide a kind of reaction unit of naphtha, to solve naphtha in the prior art
The higher problem of the thermic load of the heating furnace of reaction unit.
To achieve the goals above, according to the one aspect of the application, a kind of reaction unit of naphtha is provided, this is anti-
Answering device includes: First Heat Exchanger, for heating to naphtha；At least one high platinum reactor, above-mentioned high platinum reactor with it is upper
First Heat Exchanger connection is stated, the above-mentioned naphtha after heating, which enters in above-mentioned high platinum reactor, carries out dehydrogenation reaction, above-mentioned high platinum
Reactor includes reactor shell, and above-mentioned reactor shell has accommodating chamber, is provided with the first catalyst in above-mentioned accommodating chamber, and above-mentioned the
One catalyst includes platinum, and in above-mentioned first catalyst, and the weight content of above-mentioned platinum is greater than or equal to 80%；It is multiple to be sequentially connected in series
Reforming reactor, it is anti-that first above-mentioned reforming reactor in multiple above-mentioned reforming reactors being sequentially connected in series is that head end is reformed
Device is answered, the last one above-mentioned reforming reactor is end reforming reactor, the entrance and above-mentioned height of above-mentioned head end reforming reactor
The outlet of platinum reactor, each above-mentioned reforming reactor carry out dehydrogenation reaction to naphtha, above-mentioned end reforming reactor
Outlet is connected to the entrance of above-mentioned First Heat Exchanger, so that the output of above-mentioned end reforming reactor carries out above-mentioned naphtha
Heating.
Further, above-mentioned high platinum reactor further includes the first support portion and the second support portion, above-mentioned first support zone
In on the bottom wall of institute's accommodating chamber, on the roof of above-mentioned accommodating chamber, above-mentioned first catalyst is located at upper above-mentioned second support zone
It states between the first support portion and above-mentioned second support portion.
Further, above-mentioned first support portion and/or above-mentioned second support portion include the different alumina balls of multiple diameters.
Further, in above-mentioned first catalyst, the weight content of above-mentioned platinum is 100%.
Further, above-mentioned first catalyst is platinum ball.
Further, above-mentioned reaction unit further include: multiple heating furnaces, each above-mentioned heating furnace are located at above-mentioned high platinum reactor
Between above-mentioned end reforming reactor.
Further, above-mentioned reaction unit further include: the second heat exchanger, an entrance of above-mentioned second heat exchanger with it is above-mentioned
The outlet of the outlet of end reforming reactor, above-mentioned second heat exchanger is connected to the entrance of above-mentioned head end reforming reactor.
Further, above-mentioned reaction unit further include: circulation hydrogen pipeline connects with another entrance of above-mentioned second heat exchanger
Logical, the recycle hydrogen that the output of above-mentioned end reforming reactor output exports above-mentioned circulation hydrogen pipeline heats.
Further, above-mentioned reaction unit further includes dearsenification equipment, the outlet of above-mentioned dearsenification equipment and above-mentioned first heat exchange
The entrance of device is connected to, and above-mentioned naphtha enters in above-mentioned First Heat Exchanger after above-mentioned dearsenification equipment dearsenification.
Further, above-mentioned reaction unit includes four above-mentioned reforming reactors being sequentially connected in series, and respectively first reforms
Reactor, the second reforming reactor, third reforming reactor and fourth reforming reactor, above-mentioned head end reforming reactor are above-mentioned
First reforming reactor, above-mentioned end reforming reactor are above-mentioned fourth reforming reactor.
Using the technical solution of the application, in the reaction unit of the above-mentioned naphtha of the application, in multiple reforming reactors
Before connected one high platinum reactor, since the platinum content of catalyst is high in the high platinum reactor, so the reaction temperature needed
It is lower, it is only necessary to the output of naphtha and end reforming reactor to exchange heat, the naphtha after heating can enter
Dehydrogenation reaction is carried out into high platinum reactor, naphtha is heated without additional heating furnace, also, high platinum reactor
The reaction of part hexatomic ring dehydrating alkanes is assumed responsibility for, reduces the temperature drop of other reforming reactors, is effectively reduced, reasonable distribution respectively adds
The thermic load of hot stove improves the load of reaction unit.
Detailed description of the invention
The accompanying drawings constituting a part of this application is used to provide further understanding of the present application, and the application's shows
Meaning property embodiment and its explanation are not constituted an undue limitation on the present application for explaining the application.In the accompanying drawings:
Fig. 1 shows the structural schematic diagram of the embodiment of the reaction unit of the naphtha according to the application.
Wherein, the above drawings include the following reference numerals:
10, First Heat Exchanger；20, high platinum reactor；30, heating furnace；40, the first reforming reactor；50, it second reforms instead
Answer device；60, third reforming reactor；70, fourth reforming reactor；80, the second heat exchanger；90, hydrogen pipeline is recycled.
Specific embodiment
It is noted that following detailed description is all illustrative, it is intended to provide further instruction to the application.Unless another
It indicates, all technical and scientific terms used herein has usual with the application person of an ordinary skill in the technical field
The identical meanings of understanding.
It should be noted that term used herein above is merely to describe specific embodiment, and be not intended to restricted root
According to the illustrative embodiments of the application.As used herein, unless the context clearly indicates otherwise, otherwise singular
Also it is intended to include plural form, additionally, it should be understood that, when in the present specification using term "comprising" and/or " packet
Include " when, indicate existing characteristics, step, operation, device, component and/or their combination.
As background technique is introduced, the thermic load of the heating furnace of naphtha reaction unit in the prior art is higher,
As above in order to solve the problems, such as, present applicant proposes a kind of reaction units of naphtha.
In a kind of typical embodiment of the application, a kind of reaction unit of naphtha is provided, as shown in Figure 1, should
Reaction unit includes First Heat Exchanger 10, at least one high platinum reactor 20 and multiple reforming reactors being sequentially connected in series.Wherein,
First Heat Exchanger 10 is used to heat naphtha；Above-mentioned high platinum reactor is connected to above-mentioned First Heat Exchanger 10, upper after heating
It includes reactor shell that naphtha, which is stated, into dehydrogenation reaction, above-mentioned high platinum reactor 20 is carried out in above-mentioned high platinum reactor, above-mentioned anti-
It answers shell that there is accommodating chamber, is provided with the first catalyst in above-mentioned accommodating chamber, above-mentioned first catalyst includes platinum, and above-mentioned first
In catalyst, the weight content of above-mentioned platinum is greater than or equal to 80%；Multiple reforming reactors being sequentially connected in series, it is multiple to be sequentially connected in series
Above-mentioned reforming reactor in first above-mentioned reforming reactor be head end reforming reactor, the last one above-mentioned reforming reaction
Device be end reforming reactor, the outlet of the entrance of above-mentioned head end reforming reactor and above-mentioned high platinum reactor 20, it is each on
It states reforming reactor and dehydrogenation reaction, outlet and the above-mentioned First Heat Exchanger 10 of above-mentioned end reforming reactor is carried out to naphtha
Entrance connection, so that the output of above-mentioned end reforming reactor heats above-mentioned naphtha.Urging in reforming reactor
Agent is reforming catalyst.
In the reaction unit of the above-mentioned naphtha of the application, one high platinum bead of having connected before multiple reforming reactors is anti-
Device is answered, since the platinum content of catalyst is high in the high platinum reactor, so the reaction temperature needed is lower, it is only necessary to by naphtha
It exchanges heat with the output of end reforming reactor, the naphtha after heating, which can enter in high platinum reactor, to be taken off
Hydrogen reacts, and heats without additional heating furnace to naphtha, also, high platinum reactor assumes responsibility for the hexa-atomic cycloalkane in part
Dehydrogenation reaction reduces the temperature drop of other reforming reactors, is effectively reduced, the thermic load of each heating furnace of reasonable distribution, improves
The load of reaction unit.
In order to further ensure being stabilized for the first catalyst in the high platinum reactor, and then it ensure that high platinum reaction
The stability reacted in device, in a kind of embodiment of the application, above-mentioned high platinum reactor further includes the first support portion and second
Support part, above-mentioned first support zone on the bottom wall of institute's accommodating chamber, above-mentioned second support zone on the roof of above-mentioned accommodating chamber,
Above-mentioned first catalyst is between above-mentioned first support portion and above-mentioned second support portion.
Any can play a supporting role and right can be selected independently in the first support portion and the second support portion of the application
Dehydrogenation reaction does not have dysgenic structure and material, and those skilled in the art can select have suitable knot according to the actual situation
The first support portion and the second support portion of structure and material.
In a kind of specific embodiment of the application, above-mentioned first support portion and/or above-mentioned second support portion include multiple
The different alumina balls of diameter.Inlet oxidation aluminium ball can evenly distribute the work that naphtha feed enters the first catalyst bed
With；Outlet oxidation aluminium ball plays a part of to support the first catalyst, prevents the first catalyst from leaving high platinum with naphtha loss and reacts
Device 20 enters in head end reforming reactor.
In order to further decrease the reaction temperature in high platinum reactor, and the reaction efficiency in high platinum reactor is improved, this
In a kind of embodiment of application, the weight content of platinum is 100% in above-mentioned first catalyst.
The first above-mentioned catalyst can be any shape, and in a kind of specific embodiment, above-mentioned first catalyst is
Platinum ball.
In another embodiment of the application, as shown in Figure 1, above-mentioned reaction unit further includes multiple heating furnaces 30, it is each on
Heating furnace 30 is stated between the above-mentioned high platinum reactor being sequentially connected in series and above-mentioned end reforming reactor, heating furnace is used for counterweight
It is heated between whole reactor grade to make up reaction temperature drop.Specifically, a heating furnace 30 be located at above-mentioned high platinum reactor with it is upper
It states between head end reforming reactor, other heating furnaces are located between two above-mentioned reforming reactors being sequentially connected in series.
In order to further be effectively reduced, the thermic load of each heating furnace of reasonable distribution, further decrease the thermic load of heating furnace,
In a kind of embodiment of the application, as shown in Figure 1, above-mentioned reaction unit further includes the second heat exchanger 80, above-mentioned second heat exchanger
The outlet of 80 entrance and above-mentioned end reforming reactor, the outlet of above-mentioned second heat exchanger 80 and above-mentioned head end weight
The entrance of whole reactor is connected to.
In a kind of specific embodiment, above-mentioned reaction unit further includes circulation hydrogen pipeline 90, circulation hydrogen pipeline 90 with it is above-mentioned
Another entrance of second heat exchanger 80 is connected to, and the output of above-mentioned end reforming reactor output is to above-mentioned circulation hydrogen pipeline 90
The recycle hydrogen of output is heated, so that the temperature of recycle hydrogen increases, thus improve the mixture of recycle hydrogen and naphtha
Temperature further reduced the thermic load of heating furnace in this way.
In the another embodiment of the application, above-mentioned reaction unit further includes dearsenification equipment, the outlet of above-mentioned dearsenification equipment
It is connected to the entrance of above-mentioned First Heat Exchanger 10, above-mentioned naphtha enters above-mentioned first heat exchange after above-mentioned dearsenification equipment dearsenification
In device 10.
In another embodiment of the application, as shown in Figure 1, above-mentioned reaction unit include four be sequentially connected in series it is above-mentioned heavy
Whole reactor, respectively the first reforming reactor 40, the second reforming reactor 50, third reforming reactor 60 and fourth reforming are anti-
Device 70 is answered, above-mentioned head end reforming reactor is above-mentioned first reforming reactor 40, and above-mentioned end reforming reactor is the above-mentioned 4th
Reforming reactor 70.
Certainly, the number of the reforming reactor of the application is not limited to four, can also be other quantity, this field
Appropriate number of reforming reactor can be arranged in technical staff in reaction unit according to the actual situation.
In order to enable those skilled in the art can clearly understand the technical solution and technical effect of the application, with
Under will illustrate in conjunction with specific embodiments.
Embodiment
As shown in Figure 1, the reaction unit includes First Heat Exchanger, one high platinum reactor, four reforming reactors, four
Heating furnace, the second heat exchanger, circulation hydrogen pipeline, dearsenification device, circulating hydrogen compressor and air cooler.
The first support portion and the second support portion formed by alumina balls, above-mentioned first support are provided in high platinum reactor
Portion is located on the bottom wall of institute's accommodating chamber, and above-mentioned second support zone is on the roof of above-mentioned accommodating chamber, above-mentioned first catalyst position
Between above-mentioned first support portion and above-mentioned second support portion, and the platinum ball that the first catalyst is 100%, and the first catalyst
Total weight is 100kg.
Four above-mentioned reforming reactors be respectively the first reforming reactor 40, the second reforming reactor 50, third reform it is anti-
Device 60 and fourth reforming reactor 70 are answered, four heating furnaces are respectively the first heating furnace, the second heating furnace, third heating furnace and
Four heating furnaces.
One entrance of First Heat Exchanger 10 inputs naphtha, and the outlet of another entrance and fourth reforming reactor connects
Logical, the outlet of an entrance and fourth reforming reactor of the second heat exchanger, another entrance goes out with circulation hydrogen pipeline
Mouthful connection, a part in the output of fourth reforming reactor heat above-mentioned naphtha, another to recycle hydrogen into
Row heating.
The entrance of first heating furnace is respectively communicated with the outlet of high platinum reactor and the outlet of the second heat exchanger, and first adds
The outlet of hot stove is connected to the entrance of the first reforming reactor, the second heating furnace be used to be connected to the outlet of the first reforming reactor with
The entrance of second reforming reactor, third heating furnace are used to be connected to outlet and the third reforming reactor of the second reforming reactor
Entrance, the 4th heating furnace are used to be connected to the outlet of third reforming reactor and the entrance of fourth reforming reactor.
The entrance of circulation hydrogen pipeline is connected to circulating hydrogen compressor, the output outlet and the second heat exchange of the first heat exchange equipment
Output outlet be connected to air cooler.The connection relationship of other unaccounted consersion units is shown in the description in above content,
Details are not described herein again.
The naphtha exported from dearsenification tank is entered in high platinum reactor 20 and is carried out instead after First Heat Exchanger heats
It answers, obtained mixture and the recycle hydrogen by the heating of the second heat exchanger are mixed into the first heating furnace and heat, after heating
It entering in the first reforming reactor and reacts, obtained mixture is entered in the second heating furnace and is heated, then into
It is reacted in second reforming reactor, obtained mixture is entered in third heating furnace and heated, then into third weight
It is reacted in whole reactor, obtained mixture is entered in the 4th heating furnace and heated, and is reacted then into fourth reforming
It is reacted in device, obtained output a part enters in First Heat Exchanger, and another part enters in the second heat exchanger, cooling
Output afterwards enters cooling in air cooler.
2t/h inlet amount can be improved by reforming reaction system, and (reaction system designs inlet amount 15t/h, at present reaction feed
18.75t/h), it calculates within Nian Yunhang 7440 hours, 1.488 ten thousand tons of Nian Tigao reaction feed amount (reformer reaction liquid yield
97%), raw material naphtha per ton is processed into 1000 yuan of heavy naphtha net profit accounting of reformation: 1.488 ten thousand tons of * 97%*1000 members
=1,443 ten thousand yuan, (1443 Wan Yuanli do not deduct the depreciation of device, artificial, operating cost etc.), year device improves profit 14,430,000
Member.
The project scale of the reaction unit is 20 × 104T/a, year operate 7440 hours, and practical charging is that reformer feed is pre-
Fractionating system 40t/h, reaction feed 18.75/h, total temperature drop of four reforming reactors is not than having the reaction of high platinum reactor
Device reduces 40 DEG C, and after total temperature drop is reduced, the thermic load of heating furnace be can effectively reduce, and the inlet amount of reaction unit can be improved at least
2t/h, whole year operation 7440 hours can increase by 14,430,000 yuan of extra earning (raw material stone per ton in the 107A cycle of operation in unit year for company
Cerebrol, which is processed into 1000 yuan of heavy naphtha net profit of reformation, to be calculated: 1.488 ten thousand tons of * 97%*1000 members=14,430,000 yuan, and 14,430,000
Depreciation, the artificial, operating cost etc. of device are not deducted in member).
Since liquefaction naphtha is separated into two parts, tower top plug oil ingredient conduct by the raw material prefractionator of reaction unit
Stable light hydrocarbon product is sent into tank field, and tower bottom oil is to reform reaction feed C7+Refine naphtha component.Plug in course of normal operation
Oil ingredient stable light hydrocarbon product extracting rate substantially remains in 40% or so, after the raising of reforming reaction inlet amount, improves indirectly steady
Determine light hydrocarbon product yield, and promote raw material naphtha processing capacity, full factory's naphtha can all be digested, be solved substantially after accounting
The problem that raw material naphtha price is low and market is insufficient, and the stable light hydrocarbon component raw material naphtha that compares also has certain warp
Ji benefit, so the utility model can effectively promote the economic benefit of DCL/Direct coal liquefaction project after implementing.
It can be seen from the above description that the application the above embodiments realize following technical effect:
In the reaction unit of the above-mentioned naphtha of the application, one high platinum reaction of having connected before multiple reforming reactors
Device, since the platinum content of catalyst is high in the high platinum reactor, so the reaction temperature needed is lower, it is only necessary to by naphtha with
The output of end reforming reactor exchanges heat, and the naphtha after heating can enter in high platinum reactor and carry out dehydrogenation
It reacts, naphtha is heated without additional heating furnace, also, high platinum reactor assumes responsibility for the hexa-atomic cycloalkane in part and takes off
Hydrogen reaction, reduces the temperature drop of other reforming reactors, is effectively reduced, the thermic load of each heating furnace of reasonable distribution, improves anti-
Answer the load of device.
The foregoing is merely preferred embodiment of the present application, are not intended to limit this application, for the skill of this field
For art personnel, various changes and changes are possible in this application.Within the spirit and principles of this application, made any to repair
Change, equivalent replacement, improvement etc., should be included within the scope of protection of this application.
Claims (9)
1. a kind of reaction unit of naphtha, which is characterized in that the reaction unit includes:
First Heat Exchanger (10), for being heated to naphtha；
At least one high platinum reactor (20), the high platinum reactor (20) is connected to the First Heat Exchanger (10), after heating
The naphtha enter the high platinum reactor (20) in carry out dehydrogenation reaction, the high platinum reactor (20) includes reaction shell
Body, the reactor shell have accommodating chamber, are provided with the first catalyst in the accommodating chamber, in first catalyst, platinum
Weight content is 100%；
Multiple reforming reactors being sequentially connected in series, first in multiple reforming reactors being sequentially connected in series described reform it is anti-
Answering device is head end reforming reactor, the last one described reforming reactor is end reforming reactor, the head end reforming reaction
The outlet of the entrance of device and the high platinum reactor (20), each reforming reactor carry out dehydrogenation reaction to naphtha,
The outlet of the end reforming reactor is connected to the entrance of the First Heat Exchanger (10), so that the end reforming reactor
Output the naphtha is heated.
2. reaction unit according to claim 1, which is characterized in that the high platinum reactor further include the first support portion and
Second support portion, first support zone is on the bottom wall of institute's accommodating chamber, and second support zone is in the accommodating chamber
On roof, first catalyst is between first support portion and second support portion.
3. reaction unit according to claim 2, which is characterized in that first support portion and/or second support
Portion includes the different alumina balls of multiple diameters.
4. reaction unit according to claim 1, which is characterized in that first catalyst is platinum ball.
5. reaction unit according to claim 1, which is characterized in that the reaction unit further include:
Multiple heating furnaces (30), each heating furnace (30) be located at the high platinum reactor and the end reforming reactor it
Between.
6. reaction unit according to claim 5, which is characterized in that the reaction unit further include:
The outlet of second heat exchanger (80), the entrance and the end reforming reactor of second heat exchanger (80) connects
Logical, the outlet of second heat exchanger (80) is connected to the entrance of the head end reforming reactor.
7. reaction unit according to claim 6, which is characterized in that the reaction unit further include:
It recycles hydrogen pipeline (90), is connected to another entrance of second heat exchanger (80), the end reforming reactor is defeated
Output out heats the recycle hydrogen of circulation hydrogen pipeline (90) output.
8. reaction unit according to claim 1, which is characterized in that the reaction unit further includes dearsenification equipment, described
The outlet of dearsenification equipment is connected to the entrance of the First Heat Exchanger (10), and the naphtha is after the dearsenification equipment dearsenification
Into in the First Heat Exchanger (10).
9. reaction unit according to claim 1, which is characterized in that the reaction unit includes four institutes being sequentially connected in series
State reforming reactor, respectively the first reforming reactor (40), the second reforming reactor (50), third reforming reactor (60)
With fourth reforming reactor (70), the head end reforming reactor is first reforming reactor (40), and the end is reformed
Reactor is the fourth reforming reactor (70).
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2752382C1 (en) * | 2020-06-19 | 2021-07-26 | Общество с ограниченной ответственностью "Газпром переработка" | Method for catalytic reforming of gasoline fractions |
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2018
- 2018-11-01 CN CN201821796935.5U patent/CN209568069U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2752382C1 (en) * | 2020-06-19 | 2021-07-26 | Общество с ограниченной ответственностью "Газпром переработка" | Method for catalytic reforming of gasoline fractions |
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