CN107941047A - A kind of heat exchanger, the four Hydrogenation iso-butane device and method of mixing carbon using the heat exchanger - Google Patents
A kind of heat exchanger, the four Hydrogenation iso-butane device and method of mixing carbon using the heat exchanger Download PDFInfo
- Publication number
- CN107941047A CN107941047A CN201711164469.9A CN201711164469A CN107941047A CN 107941047 A CN107941047 A CN 107941047A CN 201711164469 A CN201711164469 A CN 201711164469A CN 107941047 A CN107941047 A CN 107941047A
- Authority
- CN
- China
- Prior art keywords
- heat exchanger
- tube
- sub
- hydrogenation
- housing
- 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.)
- Pending
Links
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/02—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being helically coiled
- F28D7/024—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being helically coiled the conduits of only one medium being helically coiled tubes, the coils having a cylindrical configuration
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/03—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of non-aromatic carbon-to-carbon double bonds
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a kind of heat exchanger, use the four Hydrogenation iso-butane device and method of mixing carbon of the heat exchanger, heat exchanger therein includes the first tube-side inlet, the outlet of the first tube side, shell side inlet and the shell-side outlet of housing, setting on the housing, it is characterised in that：At least two end sockets are interval with the housing, each end socket is enclosed at least two spaced sub- heat exchangers with corresponding housing parts, each sub- heat exchanger is sequentially arranged along the axis direction of the housing, and the first heat exchanger tube is equipped with each sub- heat exchanger；The cavity of corresponding housing between the adjacent sub- heat exchanger connects the tube side of each sub- heat exchanger, and is equipped with the second heat exchanger tube in the cavity；The second tube-side inlet and the outlet of the second tube side for connecting second heat exchanger tube are equipped with the wall of the housing corresponding to the cavity；The shell side of the adjacent sub- heat exchanger is connected by connecting tube, and the connecting tube exposes to the housing.
Description
Technical field
The present invention relates to one kind to arrive chemical plant installations and chemical process, more particularly to a kind of heat exchanger, uses the heat exchanger
Mix four Hydrogenation iso-butane device and method of carbon.
Background technology
During by mixing C_4 hydrocarbon class high-purity iso-butane, the common method of separation product has two kinds, rectification method and plus
Hydrogen method.
Wherein, rectification method is flowed back using the boiling point difference of material, so as to be separated to each component.In mixing carbon
In four, since the boiling point between C_4 hydrocarbon class each component is very close to separating difficulty is high, and cannot thoroughly remove butylene.Will
Alkene is removed to below 100g/g, using general iso-butane method of purification, such as rectification method, extraction, can not thoroughly remove alkene,
Obtained isobutane purity is poor.
Hydrogenation method is that the hydrogenation of unsaturated hydrocarbons mixed in carbon four is made iso-butane, and the catalyst that hydrogenation method uses is palladium system
Catalyst, it is expensive, and react needs and carried out in the case where pressure is more than close to 300 DEG C close to 4.0MPa, temperature, react
High energy consumption, and it is exothermic reaction to react, control difficulty is big, is easy to cause catalyst inactivation.
The content of the invention
The technical problems to be solved by the invention be for the prior art present situation provide a kind of operation flexibly, can effective profit
It is energy-saving to achieve the purpose that with the heat exchanger of out-of-bounds heat.
Another technical problem to be solved by this invention is that a kind of mixing carbon four of present situation offer for being directed to the prior art adds
The device of hydrogen iso-butane.
Another technical problem to be solved by this invention is a kind of catalyst use of present situation offer for the prior art
The good four Hydrogenation iso-butane method of mixing carbon of long lifespan, hydrogenation effect.
Technical solution is used by the present invention solves above-mentioned technical problem：The heat exchanger, including housing, be arranged on it is described
The first tube-side inlet, the outlet of the first tube side, shell side inlet and shell-side outlet on housing, it is characterised in that：
At least two end sockets are interval with the housing, each end socket is enclosed at least two with corresponding housing parts
A spaced sub- heat exchanger, each sub- heat exchanger are sequentially arranged along the axis direction of the housing, each sub- heat exchange
The first heat exchanger tube is equipped with device；
The cavity of corresponding housing between the adjacent sub- heat exchanger connects the tube side of each sub- heat exchanger, and
And it is equipped with the second heat exchanger tube in the cavity；It is equipped with corresponding to the cavity on the wall of the housing and connects second heat exchanger tube
The second tube-side inlet and the second tube side outlet；
The shell side of the adjacent sub- heat exchanger is connected by connecting tube, and the connecting tube exposes to the housing.
The end socket has two, wherein the first end of the first end socket and the housing is enclosed the first sub- heat exchanger,
The second end of second end socket and the housing is enclosed the second sub- heat exchanger.
It is preferred that first heat exchanger tube is arranged along the axial screw of the housing；Second heat exchanger tube is along the housing
Radial direction screw arrangement.Program good effect of heat exchange, can further improving heat exchanging efficiency.
Preferably, first tube-side inlet can be arranged on the bottom of the housing, and the first tube side outlet is set
At the top of the housing；
The shell side inlet is arranged on the top of the housing, and the shell-side outlet is arranged on the lower part of the housing；
First end socket is equipped with the tube side outlet of the tube side and the cavity that connect in the first sub- heat exchanger；Institute
State the tube-side inlet that the second end socket is equipped with the tube side and the cavity that connect in the second sub- heat exchanger.
The two-port of the connecting tube can be located at the lower part of the sub- heat exchanger of upstream respectively and adjacent downstream changes
The top of hot device, so as to can sufficiently be exchanged between heat transferring medium, heat transfer effect is uniform.
Use the four Hydrogenation iso-butane device of mixing carbon of above-mentioned each heat exchanger, it is characterised in that：
First tube-side inlet connects the first hydrogenation material conveyance conduit and recycle hydrogen conveyance conduit, first tube side
The second hydrogenation material conveyance conduit of outlet connection, the material of the second hydrogenation material conveyance conduit connection hydrogenation reactor enter
Mouthful, the material outlet of the hydrogenation reactor connects the shell side inlet, the material of the shell-side outlet connection hydrogenation knockout drum
Entrance；
The liquid-phase outlet connection fractionating device of the hydrogenation knockout drum；
Second heat exchanger tube connects steam conveying pipe.
Use the four Hydrogenation iso-butane method of mixing carbon of above-mentioned four Hydrogenation iso-butane device of mixing carbon, it is characterised in that
Comprise the following steps：
Four hydrogenation material of mixing carbon that temperature from upstream is 80~110 DEG C, pressure is 3.7~4.2MPaA is divided into two
Stock, wherein the first stock-traders' know-how is converged by the first hydrogenation material conveyance conduit and the recycle hydrogen from the recycle hydrogen conveyance conduit
After form reaction raw materials, from first tube-side inlet enter the described first sub- heat exchanger tube side in, with the first sub- heat exchanger
Hydrogenation products in shell side exchange heat to after 215~245 DEG C, into the shell side of the cavity；
The volume ratio of first strand of hydrogenation material and recycle hydrogen is 1：180~500；In the first sub- heat exchanger shell pass
Hydrogenation products come from the described second sub- heat exchanger；
Reaction raw materials in the cavity with second heat exchanger tube from steam heat-exchanging out-of-bounds to 230~260
Enter the second sub- heat exchanger after DEG C；
In the described second sub- heat exchanger, the material-heat-exchanging in reaction raw materials and the second sub- heat exchanger shell pass；Described second
Material in sub- heat exchanger shell pass for the temperature from the hydrogenation reactor is 290~320 DEG C, pressure is 3.2~3.7MPaA
Reaction product；
The reaction raw materials for going out the second sub- heat exchanger are mixed with second strand in the second hydrogenation material conveyance conduit
Carbon four is mixed to get the reaction feed that temperature is 285~320 DEG C, pressure is 3.5~4.0MPaA, send to the hydrogenation reactor
Under the catalysis of palladium series catalyst, hydrogenation reaction is carried out；
It is 1 to go out the reaction raw materials of the described second sub- heat exchanger and second burst of proportioning for mixing carbon four:0~5:1；
To control the reaction temperature in the hydrogenation reactor be 285~320 DEG C, pressure is 3.5~4.0MPaA；
After heat exchange, the reaction product temperature sent out from the shell-side outlet is 90~110 DEG C, pressure be 3.1~
3.6MPaA, into the hydrogenation hot knock-out pot；
Reaction product is divided into gas-liquid two-phase in hot knock-out pot, enters cold knockout drum after gas phase cooling；The cold knockout drum
The tail gas isolated goes to battery limit (BL), and the liquid phase isolated returns to the hot knock-out pot；The liquid phase of the knockout drum sends to fractionation.
The steaming that temperature is 3.0~4.0MPaG for 370~390 DEG C, pressure is preferably used into the steam in the cavity
Vapour.
Compared with prior art, heat exchanger heat exchange efficiency provided by the present invention is high, and can be readily incorporated into as needed
Out-of-bounds heat transferring medium, operation is flexible, and energy conservation and consumption reduction effects are good；The device of mixing four Hydrogenation iso-butane of carbon provided by the present invention
And method, can be high due to heat exchanger efficiency, flow setting is reasonable, and opening man-hour requirement except device uses the extra supplemental heat of heating furnace
Amount is outer, and heating furnace is not required after device normal operation, by 600,000 tons/year of scales, can save energy consumption 1500kW, and mix carbon four
After hydrogenation reaction, various types of olefins is completely converted into alkane, and the iso-butane product purity being fractionated into is up to 99.9%；It is and existing
Iso-butane product purity only 95% in technology.
Brief description of the drawings
Fig. 1 is the schematic cross-sectional view of heat exchanger in the embodiment of the present invention；
Fig. 2 is the flow diagram of the embodiment of the present invention.
Embodiment
The present invention is described in further detail below in conjunction with attached drawing embodiment.
As depicted in figs. 1 and 2, the structure of involved heat exchanger is as follows in the present embodiment：
Including housing 1, the first tube-side inlet 11 being arranged on 1 bottom of housing, the first tube side for being arranged on case top
Outlet 12, be arranged on the shell side inlet 13 of housing upper and be arranged on the shell-side outlet 14 of lower housing portion.
The interior intracavitary of housing 1 is interval with the first end socket 41 and the second end socket 42, by the inner cavity of housing be divided into longitudinal direction according to
Three regions of secondary setting.First end, that is, bottom of wherein the first end socket 41 and housing 1 is enclosed the first sub- heat exchanger
1a, the second end, that is, upper end of the second end socket 42 and housing are enclosed the second sub- heat exchanger 1b；First sub- heat exchanger 1a and
Cavity 15 is formed between second sub- heat exchanger 1b.
The first heat exchanger tube 2 is equipped with first sub- heat exchanger 1a, the entrance of first heat exchanger tube 2 connects the first tube-side inlet
11；First heat exchanger tube 2 is arranged in the first sub- heat exchanger 1a along the axial screw of housing 1.First end socket 41 is equipped with connection the
The tube side outlet of one sub- heat exchanger 1a and the tube side outlet 411 of cavity 15.
The first heat exchanger tube 2, the first tube side of outlet outlet of first heat exchanger tube 2 also are provided with second sub- heat exchanger 1b
12；First heat exchanger tube 2 is arranged in the first sub- heat exchanger 1a along the axial screw of housing 1.Second end socket 42 is equipped with connection the
The tube-side inlet 421 of two sub- heat exchanger 1b tube sides and cavity 15.
Connecting tube 5, for connecting the first sub- heat exchanger 1a shell sides and the second sub- heat exchanger 1b shell sides, port is connected to thereon
The lower part of second sub- heat exchanger 1b, its lower port connect the top of the first sub- heat exchanger.In the present embodiment, connecting tube 5 is arranged on
Outside housing 1.
Corresponding to cavity 15, the second tube-side inlet 16 and the second tube side outlet 17 are equipped with the wall of housing；In cavity 15
Equipped with the second heat exchanger tube 3, the entrance of the second heat exchanger tube 3 connects the second tube-side inlet 16, the outlet second of the second heat exchanger tube
Tube side outlet 17.
In the present embodiment, the second heat exchanger tube 3 is in cavity 15 along the radial direction screw arrangement of housing 1.
Use the four Hydrogenation iso-butane device of mixing carbon of above-mentioned heat exchanger：
First tube-side inlet 11 connects the first hydrogenation material conveyance conduit 61 and recycle hydrogen conveyance conduit 63, the first tube side go out
Mouth 12 connects the second hydrogenation material conveyance conduits 62, and the material of the second hydrogenation material conveyance conduit 62 connection hydrogenation reactor 7 enters
Mouth 71, the material outlet 72 of hydrogenation reactor 7 connect the shell side inlet 13 of heat exchanger, the connection hydrogenation of shell-side outlet 14 of heat exchanger
The material inlet of knockout drum 8.
The gas phase that hydrogenation hot knock-out pot 8 is isolated is discharged from the gaseous phase outlet at top, and 30~50 are cooled into water cooler
After DEG C, into the cold knockout drum 9 that pressure is 3.0~3.5MpaA.
The gas phase tail gas condensing that cold knockout drum 9 is isolated is to going to battery limit (BL) after 15~20 DEG C, and the liquid phase isolated is back to heat
Knockout drum 8.
The liquidus temperature that hydrogenation hot knock-out pot 8 is isolated is 50~110 DEG C, and product point is discharged from the liquid-phase outlet of bottom
Evaporate tower.
Second heat exchanger tube 3 connects steam conveying pipe 65.
Mix four Hydrogenation iso-butane method of carbon, it is characterised in that comprise the following steps：
Four hydrogenation material of mixing carbon that temperature from upstream is 80~110 DEG C, pressure is 3.7~4.2MPaA is divided into two
Stock, wherein the first stock-traders' know-how is by the first hydrogenation material conveyance conduit 61 and shape after the recycle hydrogen confluence from recycle hydrogen conveyance conduit 63
Into reaction raw materials, enter from the first tube-side inlet 11 in the tube side of the first sub- heat exchanger 1a, in the first sub- heat exchanger 1a shell sides
Hydrogenation products exchange heat to after 215~245 DEG C, into the shell side of cavity 15；
In the present embodiment, the quality group of mixing four hydrogenation material of carbon becomes：Methane 0.01%, ethane 0.54%, propane
8.5%th, iso-butane 66.37%, normal butane 19.12%, isobutene 0.81%, 1- butylene 2.29%, cis-2-butene 0.06%,
Trans-2-butene 1.59%, C_5 olefins 0.40%, C 5 alkane 0.19%, thiophene 0.02%, water 0.01%.
The composition of hydrogenation material and the mixed reaction raw materials of recycle hydrogen is：Hydrogen 2.70%, hydrogen sulfide 0.01%, methane
0.93%th, ethane 1.31%, propane 10.77%, iso-butane 62.84%, normal butane 17.32%, isobutene 0.62%, 1- butylene
1.73%th, cis-2-butene 0.05%, Trans-2-butene 1.20%, C_5 olefins 0.30%, C 5 alkane 0.17%, thiophene
0.02%th, water 0.03%.The volume ratio of control loop hydrogen and first strand of hydrogenation material is 180~500, the present embodiment 350；The
Hydrogenation products in one sub- heat exchanger 1a shell sides come from the second sub- heat exchanger 1b；
Reaction raw materials in the cavity 15 with the second heat exchanger tube 3 from steam heat-exchanging out-of-bounds to 230~260 DEG C it is laggard
Enter the second sub- heat exchanger 1b；
In the second sub- heat exchanger 1b, the material-heat-exchanging in reaction raw materials and the second sub- heat exchanger 1b shell sides；Second son changes
Material in hot device 1b shell sides is the reaction that the temperature from hydrogenation reactor is 290~320 DEG C, pressure is 3.2~3.7MPaA
Product；
The reaction raw materials for going out the second sub- heat exchanger 1b mix carbon with second strand in the second hydrogenation material conveyance conduit
Four are mixed to get the reaction feed that temperature is 285~320 DEG C, pressure is 3.5~4.0MPaA, send to hydrogenation reactor 7 in palladium system
Under the catalysis of catalyst, hydrogenation reaction is carried out；
It is 1 to go out the reaction raw materials of the second sub- heat exchanger 1b and second burst of proportioning for mixing carbon four:0~5:1；
To control the reaction temperature in the hydrogenation reactor be 285~320 DEG C, pressure is 3.5~4.0MPaA；
After heat exchange, the reaction product temperature from shell-side outlet submitting is 90~110 DEG C, pressure is 3.1~3.6MPaA, into
Enter to be hydrogenated with hot knock-out pot 8；It is 1 to control liquid-gas ratio example in hydrogenation hot knock-out pot:1~2:1.
Reaction product is divided into gas-liquid two-phase in hot knock-out pot 8, and gas phase removes water cooler at the top of hot knock-out pot, laggard cold point
From tank 9, the gas phase tail gas that cold knockout drum 9 is isolated goes to battery limit (BL), and the liquid phase isolated returns to hot knock-out pot；
The gas phase prevailing quality isolated from hot knock-out pot 8 forms：Hydrogen 4.58%, hydrogen sulfide 0.03%, methane
1.62%th, ethane 2.08%, propane 14.07%, iso-butane 60.68%, normal butane 16.65%, C 5 alkane 0.24%, water
0.06% (mass fraction),
The liquid phase prevailing quality of hot knock-out pot discharge, which forms, is：Hydrogen 0.11%, hydrogen sulfide 0.01%, methane 0.12%,
Ethane 0.52%, propane 8.41%, iso-butane 67.04%, normal butane 23.18%, C 5 alkane 0.60%, water 0.01%, from
Send to fractionating column in knockout drum bottom.
From the above, it is seen that after mixing four hydrogenation reaction of carbon, various types of olefins is completely converted into alkane.
The iso-butane product purity for being fractionated into going out after tower fractionation is up to 99.9%；And iso-butane product purity in the prior art
Only 95%.
Also, the application only needs to use heating furnace 10 when device goes into operation non-output hydrogenation reaction product, in device just
Often, by 600,000 tons/year of scales, energy consumption 1500kW can be saved without heating furnace 10 after operation.
And ordinary heat exchanger used in the prior art, heat exchange efficiency are low, it is extra that when normal operation, needs heating furnace to provide
Heat, high energy consumption.
Claims (8)
1. a kind of heat exchanger, including housing (1), the first tube-side inlet (11), the first tube side that are arranged on the housing (1) go out
Mouth (12), shell side inlet (13) and shell-side outlet (14), it is characterised in that：
At least two end sockets are interval with the housing (1), each end socket is enclosed at least two with corresponding housing parts
A spaced sub- heat exchanger, each sub- heat exchanger are sequentially arranged along the axis direction of the housing (1), and each son changes
The first heat exchanger tube (2) is equipped with hot device；
The cavity (15) of corresponding housing between the adjacent sub- heat exchanger connects the tube side of each sub- heat exchanger, and
And it is equipped with the second heat exchanger tube (3) in the cavity (15)；Connection institute is equipped with the wall of the housing corresponding to the cavity (15)
State the second tube-side inlet (16) and the second tube side outlet (17) of the second heat exchanger tube (3)；
The shell side of the adjacent sub- heat exchanger is connected by connecting tube (4), and the connecting tube (5) exposes to the housing
(1)。
2. heat exchanger according to claim 1, it is characterised in that the end socket has two, wherein the first end socket (41) and institute
The first end for stating housing (1) is enclosed the first sub- heat exchanger (1a), the second end of the second end socket (42) and the housing
It is enclosed the second sub- heat exchanger (1b).
3. heat exchanger according to claim 1 or 2, it is characterised in that first heat exchanger tube (2) is along the housing (1)
Axial screw is arranged；Radial direction screw arrangement of second heat exchanger tube (3) along the housing (1).
4. heat exchanger according to claim 3, it is characterised in that first tube-side inlet (11) is arranged on the housing
(1) bottom, the first tube side outlet (12) are arranged on the top of the housing (1)；
The shell side inlet (13) is arranged on the top of the housing (1), and the shell-side outlet (14) is arranged on the housing (1)
Lower part；
First end socket (41) is equipped with the pipe of the tube side and the cavity (15) that connect in the first sub- heat exchanger (1a)
Journey exports (411)；Second end socket (42) is equipped with tube side and the cavity connected in the second sub- heat exchanger (1b)
(15) tube-side inlet (421).
5. heat exchanger according to claim 4, it is characterised in that the two-port of the connecting tube (5) is respectively positioned at upstream
The lower part of the sub- heat exchanger and the top of the sub- heat exchanger of adjacent downstream.
6. the four Hydrogenation iso-butane device of mixing carbon of the heat exchanger as described in claim 1 to 5 any claim is used, its
It is characterized in that：
First tube-side inlet (11) connects the first hydrogenation material conveyance conduit (61) and recycle hydrogen conveyance conduit (63), described
First tube side outlet (12) connects the second hydrogenation material conveyance conduit (62), the second hydrogenation material conveyance conduit (62) connection
The material inlet (71) of hydrogenation reactor (7), the material outlet (72) of the hydrogenation reactor (7) connect the shell side inlet
(13), the material inlet of shell-side outlet (14) the connection hydrogenation knockout drum (8)；
The liquid-phase outlet connection fractionating device of the hydrogenation knockout drum (8)；
Second heat exchanger tube (3) the connection steam conveying pipe (65).
7. use the four Hydrogenation iso-butane side of mixing carbon of mixing four Hydrogenation iso-butane device of carbon as claimed in claim 6
Method, it is characterised in that comprise the following steps：
Four hydrogenation material of mixing carbon that temperature from upstream is 80~110 DEG C, pressure is 3.7~4.2MPaA is divided into two strands, its
In the first stock-traders' know-how by the first hydrogenation material conveyance conduit (61) with from the recycle hydrogen conveyance conduit (63) recycle hydrogen
Reaction raw materials are formed after confluence, enter from first tube-side inlet (11) in the tube side of the described first sub- heat exchanger (1a), with
Hydrogenation products in first sub- heat exchanger (1a) shell side exchange heat to after 215~245 DEG C, into the shell side of the cavity (15)；
The volume ratio of first strand of hydrogenation material and recycle hydrogen is 1：180~500；In first sub- heat exchanger (1a) shell side
Hydrogenation products come from the described second sub- heat exchanger (1b)；
Reaction raw materials in the cavity (15) with second heat exchanger tube (3) from steam heat-exchanging out-of-bounds to 230~
Enter the second sub- heat exchanger (1b) after 260 DEG C；
In the described second sub- heat exchanger (1b), the material-heat-exchanging in reaction raw materials and the second sub- heat exchanger (1b) shell side；It is described
Material in second sub- heat exchanger (1b) shell side for the temperature from the hydrogenation reactor is 290~320 DEG C, pressure 3.2
The reaction product of~3.7MPaA；
The reaction raw materials for going out the second sub- heat exchanger (1b) are mixed with second strand in the second hydrogenation material conveyance conduit
Carbon four is mixed to get the reaction feed that temperature is 285~320 DEG C, pressure is 3.5~4.0MPaA, send to the hydrogenation reactor
(7) under the catalysis of palladium series catalyst, hydrogenation reaction is carried out；
It is 1 to go out the reaction raw materials of the described second sub- heat exchanger (1b) and second burst of proportioning for mixing carbon four:0~5:1；
To control the reaction temperature in the hydrogenation reactor be 285~320 DEG C, pressure is 3.5~4.0MPaA；
After heat exchange, the reaction product temperature from shell-side outlet submitting is 90~110 DEG C, pressure is 3.1~3.6MPaA, into
Enter the hydrogenation hot knock-out pot (8)；
Reaction product is divided into gas-liquid two-phase in hot knock-out pot (8), enters cold knockout drum (9) after gas phase cooling；The cold separation
The tail gas that tank (9) is isolated goes to battery limit (BL), and the liquid phase isolated returns to the hot knock-out pot (8)；The liquid phase of the knockout drum (8) is sent
Go to be fractionated.
8. mixing four Hydrogenation iso-butane method of carbon according to claim 7, it is characterised in that enter the cavity (15)
Interior vapor (steam) temperature is 370~390 DEG C, pressure is 3.0~4.0MPaG.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711164469.9A CN107941047A (en) | 2017-11-21 | 2017-11-21 | A kind of heat exchanger, the four Hydrogenation iso-butane device and method of mixing carbon using the heat exchanger |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711164469.9A CN107941047A (en) | 2017-11-21 | 2017-11-21 | A kind of heat exchanger, the four Hydrogenation iso-butane device and method of mixing carbon using the heat exchanger |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107941047A true CN107941047A (en) | 2018-04-20 |
Family
ID=61929461
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711164469.9A Pending CN107941047A (en) | 2017-11-21 | 2017-11-21 | A kind of heat exchanger, the four Hydrogenation iso-butane device and method of mixing carbon using the heat exchanger |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107941047A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112254552A (en) * | 2020-11-10 | 2021-01-22 | 镇海石化建安工程有限公司 | Heat exchange system and heat exchange process for aluminum oxide smelting |
| CN113063310A (en) * | 2021-04-30 | 2021-07-02 | 镇海石化建安工程有限公司 | Hydrogenation heat exchange system and heat exchange process adopting multi-strand wound tube type heat exchanger |
| CN113063309A (en) * | 2021-04-30 | 2021-07-02 | 镇海石化建安工程有限公司 | Hydrogenation heat exchange system and heat exchange process adopting multi-strand wound tube type heat exchanger |
| CN113091498A (en) * | 2021-04-30 | 2021-07-09 | 镇海石化建安工程有限公司 | Hydrogenation heat exchange system and heat exchange process adopting multi-strand wound tube type heat exchanger |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101747933A (en) * | 2008-11-28 | 2010-06-23 | 中国石油化工股份有限公司 | Modifying method for naphtha and light hydrocarbon aromatization |
| CN103509600A (en) * | 2012-06-21 | 2014-01-15 | 中国石油天然气股份有限公司 | Method for producing high-octane gasoline blending component by mixed carbon four-hydrocarbon aromatization |
| CN203389623U (en) * | 2013-06-28 | 2014-01-15 | 中国石油天然气集团公司 | Liquid-phase hydrogenation reaction system |
| CN107062951A (en) * | 2017-05-31 | 2017-08-18 | 镇海石化建安工程有限公司 | A kind of heat exchanger group |
| CN207816054U (en) * | 2017-11-21 | 2018-09-04 | 宁波东鼎石化装备有限公司 | A kind of heat exchanger, the four Hydrogenation iso-butane device of mixing carbon using the heat exchanger |
-
2017
- 2017-11-21 CN CN201711164469.9A patent/CN107941047A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101747933A (en) * | 2008-11-28 | 2010-06-23 | 中国石油化工股份有限公司 | Modifying method for naphtha and light hydrocarbon aromatization |
| CN103509600A (en) * | 2012-06-21 | 2014-01-15 | 中国石油天然气股份有限公司 | Method for producing high-octane gasoline blending component by mixed carbon four-hydrocarbon aromatization |
| CN203389623U (en) * | 2013-06-28 | 2014-01-15 | 中国石油天然气集团公司 | Liquid-phase hydrogenation reaction system |
| CN107062951A (en) * | 2017-05-31 | 2017-08-18 | 镇海石化建安工程有限公司 | A kind of heat exchanger group |
| CN207816054U (en) * | 2017-11-21 | 2018-09-04 | 宁波东鼎石化装备有限公司 | A kind of heat exchanger, the four Hydrogenation iso-butane device of mixing carbon using the heat exchanger |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112254552A (en) * | 2020-11-10 | 2021-01-22 | 镇海石化建安工程有限公司 | Heat exchange system and heat exchange process for aluminum oxide smelting |
| CN112254552B (en) * | 2020-11-10 | 2024-05-31 | 镇海石化建安工程股份有限公司 | Heat exchange system and heat exchange process for aluminum oxide smelting |
| CN113063310A (en) * | 2021-04-30 | 2021-07-02 | 镇海石化建安工程有限公司 | Hydrogenation heat exchange system and heat exchange process adopting multi-strand wound tube type heat exchanger |
| CN113063309A (en) * | 2021-04-30 | 2021-07-02 | 镇海石化建安工程有限公司 | Hydrogenation heat exchange system and heat exchange process adopting multi-strand wound tube type heat exchanger |
| CN113091498A (en) * | 2021-04-30 | 2021-07-09 | 镇海石化建安工程有限公司 | Hydrogenation heat exchange system and heat exchange process adopting multi-strand wound tube type heat exchanger |
| CN113063310B (en) * | 2021-04-30 | 2024-05-24 | 镇海石化建安工程股份有限公司 | Hydrogenation heat exchange system and heat exchange process adopting multi-strand winding tubular heat exchanger |
| CN113091498B (en) * | 2021-04-30 | 2024-05-24 | 镇海石化建安工程股份有限公司 | Hydrogenation heat exchange system and heat exchange process adopting multi-strand winding tubular heat exchanger |
| CN113063309B (en) * | 2021-04-30 | 2024-06-04 | 镇海石化建安工程股份有限公司 | Hydrogenation heat exchange system and heat exchange process adopting multi-strand winding tubular heat exchanger |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107941047A (en) | A kind of heat exchanger, the four Hydrogenation iso-butane device and method of mixing carbon using the heat exchanger | |
| CN207816054U (en) | A kind of heat exchanger, the four Hydrogenation iso-butane device of mixing carbon using the heat exchanger | |
| US11148955B2 (en) | Synthesis device and method for producing a product | |
| CN102766021B (en) | Production system and production method for continuously producing ethanol by ethyl acetate through using hydrogenation | |
| CN105399604B (en) | A kind of energy-saving ultra-large methane synthesizing method and device producing different brackets steam | |
| CN105944652A (en) | Tubular micro-channel alkylation reactor and application method thereof | |
| CN110218151B (en) | Device and method for preparing propyl propionate through tower kettle flash evaporation type heat pump reaction rectification | |
| CN109012742B (en) | Catalyst for catalytic cracking of naphtha, preparation method and application | |
| CN103240036A (en) | Temperature stress resistant heat transfer reactor and composite device and application thereof | |
| CN106955648A (en) | Tubular reaction system for gas-solid-liquid three-phase highly exothermic reaction | |
| CN101898930B (en) | Device for producing cyclohexane by adding hydrogen in benzene and synthesis process | |
| CN205295183U (en) | Energy -saving ultra -large methanol synthesis device of production different brackets steam | |
| CN210560278U (en) | Hydrocracking and hydrodesulfurization integrated unit | |
| CN206793615U (en) | Tubular reaction system for gas-solid-liquid three-phase highly exothermic reaction | |
| CN206069360U (en) | A kind of heat exchange of energy-conserving and environment-protective and condenser system | |
| CN107937022A (en) | Pyrolysis gasoline hydrogenation device and method | |
| CN205235936U (en) | Modular fixed bed reactor reaches device by its formation | |
| CN207608526U (en) | pyrolysis gasoline hydrogenation device | |
| CN204265660U (en) | A kind of device of the hydrogen circulation amount reduced in hydrogenation process | |
| CN103517889A (en) | Exchanger and a process relating thereto | |
| CN217854621U (en) | Succinic anhydride refining system | |
| CN219024231U (en) | Disproportionation device reactor feeding system | |
| CN204958828U (en) | A reactor for alkylate is synthetic | |
| CN204958826U (en) | A reactor for alkylate is synthetic | |
| CN213493686U (en) | Hydroxyl ether reaction system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20190617 Address after: 315207 Jiaochuan Street Refining Road, Zhenhai District, Ningbo City, Zhejiang Province Applicant after: ZHENHAI PETROCHEMICAL JIANAN ENGINEERING Co.,Ltd. Address before: 315207 Jiaochuan Street Refining Road, Zhenhai District, Ningbo City, Zhejiang Province Applicant before: NINGBO DONGDING PETROCHEMICAL EQUIPMENT Co.,Ltd. |
|
| TA01 | Transfer of patent application right | ||
| CB02 | Change of applicant information |
Address after: 315207 Jiaochuan Street Refining Road, Zhenhai District, Ningbo City, Zhejiang Province Applicant after: Zhenhai Petrochemical Construction and Installation Engineering Co.,Ltd. Address before: 315207 Jiaochuan Street Refining Road, Zhenhai District, Ningbo City, Zhejiang Province Applicant before: ZHENHAI PETROCHEMICAL JIANAN ENGINEERING Co.,Ltd. |
|
| CB02 | Change of applicant information |