CN207816054U - A kind of heat exchanger, the four Hydrogenation iso-butane device of mixing carbon using the heat exchanger - Google Patents
A kind of heat exchanger, the four Hydrogenation iso-butane device of mixing carbon using the heat exchanger Download PDFInfo
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- CN207816054U CN207816054U CN201721561364.2U CN201721561364U CN207816054U CN 207816054 U CN207816054 U CN 207816054U CN 201721561364 U CN201721561364 U CN 201721561364U CN 207816054 U CN207816054 U CN 207816054U
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Abstract
The utility model is related to a kind of heat exchanger, use the four Hydrogenation iso-butane device 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 shell, setting on the housing, it is characterised in that：At least two end sockets are equipped at intervals in the shell, 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 shell, and the first heat exchanger tube is equipped in each sub- heat exchanger；The cavity of corresponding shell between the adjacent sub- heat exchanger is connected to the tube side of each sub- heat exchanger, and the second heat exchanger tube is equipped in the cavity；The second tube-side inlet and the outlet of the second tube side for being connected to second heat exchanger tube are equipped on the wall of the shell 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 shell.
Description
Technical field
The utility model is related to one kind to chemical plant installations and chemical process more particularly to a kind of heat exchanger, use the heat exchange
The four Hydrogenation iso-butane device of mixing carbon of device.
Background technology
When by mixing C_4 hydrocarbon class high-purity iso-butane, there are two ways to separation product is often used, rectification method and plus
Hydrogen method.
Wherein, rectification method is flowed back using the boiling point difference of substance, to be detached 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.It will
Alkene is removed to 100g/g hereinafter, 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 iso-butane is made in the hydrogenation of unsaturated hydrocarbons mixed in carbon four, and the catalyst that hydrogenation method uses is palladium system
Catalyst, it is expensive, and react and need to carry out in the case where pressure is more than close to 4.0MPa, temperature close to 300 DEG C, it reacts
High energy consumption, and it is exothermic reaction to react, control difficulty is big, is easy to cause catalyst inactivation.
Invention content
Technical problem to be solved in the utility model be for the prior art present situation provide it is a kind of operation flexibly, can have
Effect utilizes the heat exchanger of out-of-bounds heat, energy-saving to achieve the purpose that.
Another technical problem to be solved in the utility model is a kind of mixing carbon of present situation offer for the prior art
The device of four Hydrogenation iso-butanes.
Technical solution is used by the utility model solves above-mentioned technical problem：The heat exchanger, including shell, setting exist
The first tube-side inlet, the outlet of the first tube side, shell side inlet on the shell and shell-side outlet, it is characterised in that：
At least two end sockets are equipped at intervals in the shell, 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 shell, each sub- heat exchange
The first heat exchanger tube is equipped in device；
The cavity of corresponding shell between the adjacent sub- heat exchanger is connected to the tube side of each sub- heat exchanger, and
And the second heat exchanger tube is equipped in the cavity；It is equipped on the wall of the shell corresponding to the cavity and is connected to 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 shell.
There are two the end sockets, wherein the first end of the first end socket and the shell is enclosed the first sub- heat exchanger,
The second end of second end socket and the shell is enclosed the second sub- heat exchanger.
It is preferred that first heat exchanger tube is arranged along the axial screw of the shell；Second heat exchanger tube is along the shell
Radial screw arrangement.Program good effect of heat exchange, can further improving heat exchanging efficiency.
Preferably, first tube-side inlet can be arranged in the bottom of the shell, the first tube side outlet setting
At the top of the shell；
The shell side inlet is arranged on the top of the shell, and the shell-side outlet is arranged in the lower part of the shell；
First end socket is equipped with the tube side outlet of the tube side and the cavity that are connected 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 are connected 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 and adjacent downstream changes
The top of hot device, so as to can adequately 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 material of the second hydrogenation material conveyance conduit of outlet connection, the second hydrogenation material conveyance conduit connection hydrogenation reactor enters
Mouthful, the material outlet of the hydrogenation reactor connects the material of the shell side inlet, the shell-side outlet connection plus hydrogen knockout drum
Entrance；
Described plus hydrogen knockout drum liquid-phase outlet connects fractionating device；
Second heat exchanger tube connects steam conveying pipe.
Use the four Hydrogenation iso-butane method of mixing carbon of four Hydrogenation iso-butane device of above-mentioned mixing carbon, it is characterised in that
Include 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 in 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 be the temperature from the hydrogenation reactor be 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；
The proportioning that the reaction raw materials for going out the described second sub- heat exchanger mix carbon four with second strand is 1:0~5:1；
Control that the reaction temperature in the hydrogenation reactor is 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 heat from hydrogenation knockout drum；
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 utility model is high, and can as needed easily
Out-of-bounds heat transferring medium is introduced, operation is flexible, and energy conservation and consumption reduction effects are good；Four Hydrogenation isobutyl of mixing carbon provided by the utility model
The device and method of alkane, can be due to heat exchanger efficiency height, and flow setting is reasonable, and opening man-hour requirement except device uses heating furnace volume
Outside outer additional heat, heating furnace is not needed after device normal operation, by 600,000 tons/year of scales, energy consumption 1500kW can be saved, and
After mixing four hydrogenation reaction of carbon, various types of olefins is completely converted into alkane, and the iso-butane product purity being fractionated into is up to
99.9%；And iso-butane product purity only 95% in the prior art.
Description of the drawings
Fig. 1 is the schematic cross-sectional view of heat exchanger in the utility model embodiment；
Fig. 2 is the flow diagram of the utility model embodiment.
Specific implementation mode
The utility model 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 shell 1, the first tube-side inlet 11 being arranged on 1 bottom of shell, the first tube side in case top is set
The shell-side outlet 14 of shell side inlet 13 and setting in the lower part of the housing of outlet 12, setting in the upper housing.
The interior intracavitary of shell 1 is equipped at intervals with the first end socket 41 and the second end socket 42, by the inner cavity of shell be divided into it is longitudinal according to
Three regions of secondary setting.First end, that is, lower end of wherein the first end socket 41 and shell 1 is enclosed the first sub- heat exchanger
The second end, that is, upper end of 1a, the second end socket 42 and shell 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 in first sub- heat exchanger 1a, the entrance of first heat exchanger tube 2 is connected to 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 shell 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 in 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 shell 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 being connected to 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, lower port connect the top of the first sub- heat exchanger.In the present embodiment, the setting of connecting tube 5 exists
Outside shell 1.
Corresponding to cavity 15, the second tube-side inlet 16 and the second tube side outlet 17 are equipped on the wall of shell；In cavity 15
Equipped with the second heat exchanger tube 3, the entrance of the second heat exchanger tube 3 is connected to 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 screw arrangement of shell 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 of shell-side outlet 14 of heat exchanger plus hydrogen
The material inlet of knockout drum 8.
The gas phase that heat from hydrogenation knockout drum 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 heat from hydrogenation knockout drum 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 include 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
At reaction raw materials, out of, the first tube-side inlet 11 enters the first sub- heat exchanger 1a tube side, 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%, 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 group of hydrogenation material and the mixed reaction raw materials of recycle hydrogen becomes：Hydrogen 2.70%, hydrogen sulfide 0.01%, methane
0.93%, ethane 1.31%, propane 10.77%, iso-butane 62.84%, normal butane 17.32%, isobutene 0.62%, 1- butylene
1.73%, cis-2-butene 0.05%, Trans-2-butene 1.20%, C_5 olefins 0.30%, C 5 alkane 0.17%, thiophene
0.02%, 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 in 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；
The proportioning that the reaction raw materials for going out the second sub- heat exchanger 1b mix carbon four with second strand is 1:0~5:1；
Control that the reaction temperature in the hydrogenation reactor is 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 heat from hydrogenation knockout drum 8；It is 1 to control liquid-gas ratio example in heat from hydrogenation knockout drum: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 group isolated from hot knock-out pot 8 becomes：Hydrogen 4.58%, hydrogen sulfide 0.03%, methane
1.62%, 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 group of hot knock-out pot discharge becomes：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.
It is fractionated into the iso-butane product purity gone out after tower fractionation and is up to 99.9%；And iso-butane product purity in the prior art
Only 95%.
Also, the application only needed when device goes into operation non-output hydrogenation reaction product use heating furnace 10, device just
Often energy consumption 1500kW can be saved by 600,000 tons/year of scales after operation without heating furnace 10.
And ordinary heat exchanger used in the prior art, heat exchange efficiency are low, it is additional that when normal operation, needs heating furnace to provide
Heat, high energy consumption.
Claims (6)
1. a kind of heat exchanger, including the first tube-side inlet (11), the first tube side of shell (1), setting on the shell (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 equipped at intervals in the shell (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 shell (1), and each son changes
The first heat exchanger tube (2) is equipped in hot device；
The cavity (15) of corresponding shell between the adjacent sub- heat exchanger is connected to the tube side of each sub- heat exchanger, and
And the second heat exchanger tube (3) is equipped in the cavity (15)；Connection institute is equipped on the wall of the shell 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 (5), and the connecting tube (5) exposes to the shell
(1)。
2. heat exchanger according to claim 1, it is characterised in that there are two the end sockets, wherein the first end socket (41) and institute
The first end for stating shell (1) is enclosed the first sub- heat exchanger (1a), the second end of the second end socket (42) and the shell
It is enclosed the second sub- heat exchanger (1b).
3. heat exchanger according to claim 2, it is characterised in that axis of first heat exchanger tube (2) along the shell (1)
To screw arrangement；Radial screw arrangement of second heat exchanger tube (3) along the shell (1).
4. heat exchanger according to claim 3, it is characterised in that first tube-side inlet (11) is arranged in the shell
(1) bottom, top of the first tube side outlet (12) setting in the shell (1)；
On the top of the shell (1), the shell-side outlet (14) is arranged in the shell (1) for shell side inlet (13) setting
Lower part；
First end socket (41) is equipped with the pipe of the tube side and the cavity (15) that are connected in the first sub- heat exchanger (1a)
Journey exports (411)；Second end socket (42) is equipped with the tube side being connected in the second sub- heat exchanger (1b) and the cavity
(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 located at upstream
The top of the lower part and the sub- heat exchanger of adjacent downstream of the sub- heat exchanger.
6. using the four Hydrogenation iso-butane device of mixing carbon of heat exchanger according to any one of claims 1 to 5,
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 exports (12) and connects the second hydrogenation material conveyance conduit (62), the second hydrogenation material conveyance conduit (62) connection
The material outlet (72) of the material inlet (71) of hydrogenation reactor (7), the hydrogenation reactor (7) connects the shell side inlet
(13), the material inlet of shell-side outlet (14) connection plus hydrogen knockout drum (8)；
Described plus hydrogen knockout drum (8) liquid-phase outlet connects fractionating device；
Second heat exchanger tube (3) the connection steam conveying pipe (65).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721561364.2U CN207816054U (en) | 2017-11-21 | 2017-11-21 | A kind of heat exchanger, the four Hydrogenation iso-butane device of mixing carbon using the heat exchanger |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721561364.2U CN207816054U (en) | 2017-11-21 | 2017-11-21 | A kind of heat exchanger, the four Hydrogenation iso-butane device of mixing carbon using the heat exchanger |
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| Publication Number | Publication Date |
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| CN207816054U true CN207816054U (en) | 2018-09-04 |
Family
ID=63334125
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| Application Number | Title | Priority Date | Filing Date |
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| CN201721561364.2U Active CN207816054U (en) | 2017-11-21 | 2017-11-21 | A kind of heat exchanger, the four Hydrogenation iso-butane device of mixing carbon using the heat exchanger |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107941047A (en) * | 2017-11-21 | 2018-04-20 | 宁波东鼎石化装备有限公司 | A kind of heat exchanger, the four Hydrogenation iso-butane device and method of mixing carbon using the heat exchanger |
| 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 |
-
2017
- 2017-11-21 CN CN201721561364.2U patent/CN207816054U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107941047A (en) * | 2017-11-21 | 2018-04-20 | 宁波东鼎石化装备有限公司 | A kind of heat exchanger, the four Hydrogenation iso-butane device and method of mixing carbon using the heat exchanger |
| 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 |
| 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 |
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| GR01 | Patent grant | ||
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| TR01 | Transfer of patent right |
Effective date of registration: 20190618 Address after: 315207 Jiaochuan Street Refining Road, Zhenhai District, Ningbo City, Zhejiang Province Patentee after: ZHENHAI PETROCHEMICAL JIANAN ENGINEERING Co.,Ltd. Address before: 315207 Jiaochuan Street Refining Road, Zhenhai District, Ningbo City, Zhejiang Province Patentee before: NINGBO DONGDING PETROCHEMICAL EQUIPMENT Co.,Ltd. |
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| CP01 | Change in the name or title of a patent holder | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 315207 Jiaochuan Street Refining Road, Zhenhai District, Ningbo City, Zhejiang Province Patentee after: Zhenhai Petrochemical Construction and Installation Engineering Co.,Ltd. Address before: 315207 Jiaochuan Street Refining Road, Zhenhai District, Ningbo City, Zhejiang Province Patentee before: ZHENHAI PETROCHEMICAL JIANAN ENGINEERING Co.,Ltd. |