CN207608526U - pyrolysis gasoline hydrogenation device - Google Patents
pyrolysis gasoline hydrogenation device Download PDFInfo
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- CN207608526U CN207608526U CN201721565838.0U CN201721565838U CN207608526U CN 207608526 U CN207608526 U CN 207608526U CN 201721565838 U CN201721565838 U CN 201721565838U CN 207608526 U CN207608526 U CN 207608526U
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Abstract
The utility model is related to a kind of pyrolysis gasoline hydrogenation device, device includes hydrogenation reactor and heat exchanger, it is characterised in that：The heat exchanger includes heat exchanger and preheater；Wherein, the tube-side inlet of the heat exchanger connects the tube side outlet of the preheater；The tube-side inlet of the preheater connects the first hydrogenation material conveyance conduit and first circulation hydrogen conveyance conduit, the second hydrogenation material conveyance conduit of tube side outlet connection of the heat exchanger, the first material entrance of the second hydrogenation material conveyance conduit connection hydrogenation reactor, second circulation hydrogen conveyance conduit connects the second material entrance of the hydrogenation reactor, the material outlet connection first branch and the second branch of the hydrogenation reactor；Wherein the first branch connects the shell side inlet of the heat exchanger, and the shell-side outlet of the heat exchanger connects the material inlet of hydrogenation products knockout drum after converging with the second branch.
Description
Technical field
The utility model is related to one kind to chemical plant installations and chemical process more particularly to a kind of pyrolysis gasoline hydrogenation devices.
Background technology
Cracking of ethylene gasoline contains a large amount of unsaturated hydrocarbons, so property is extremely unstable, is easy to generate colloid, polymerize
Reaction, it is necessary to storage and following process can be carried out after hydrofinishing.
Hydrocracking gasoline is using the raw pyrolysis gasoline of ethylene unit by-product as raw material, by two-stage hydrogenation technique productions C6
~C8 hydrogasolines.The purpose of wherein one-stage hydrogenation is alkadienes, including chain, cyclic diene hydrocarbon and alkenyl aroma race such as benzene
The hydrogenation of olefins such as ethylene, while part monoolefin hydrogenation at saturated hydrocarbons.The purpose of secondary hydrogenation reaction is that one-stage hydrogenation is given birth to
At alkene carry out again plus hydrogen, while desulfurization.
Since one-stage hydrogenation reaction temperature is at 40 DEG C or so, secondary hydrogenation reaction temperature is then up to 240 DEG C, between the two
The temperature difference is larger, and reaction mass needs to be preheated using more heat exchangers before entering second-stage hydrogenation reactor, equipment investment
Greatly, it is piped quantity and installation area is also big, and high energy consumption.
Invention content
Technical problem to be solved in the utility model is to provide that a kind of equipment investment is low, changes for the present situation of the prior art
The pyrolysis gasoline hydrogenation device that the thermal efficiency is high, energy conservation and consumption reduction effects are good.
Technical solution is used by the utility model solves above-mentioned technical problem：The pyrolysis gasoline hydrogenation device, including
Hydrogenation reactor and heat exchanger, it is characterised in that：
The heat exchanger includes heat exchanger and preheater；
Wherein, the tube-side inlet of the heat exchanger connects the tube side outlet of the preheater；
The tube-side inlet of the preheater connects the first hydrogenation material conveyance conduit and first circulation hydrogen conveyance conduit, described
The second hydrogenation material conveyance conduit of tube side outlet connection of heat exchanger, the second hydrogenation material conveyance conduit connect hydrogenation reaction
The first material entrance of device, second circulation hydrogen conveyance conduit connect the second material entrance of the hydrogenation reactor, described plus hydrogen
The material outlet connection first branch and the second branch of reactor；Wherein the first branch connects the shell side inlet of the heat exchanger,
The shell-side outlet of the heat exchanger connects the material inlet of hydrogenation products knockout drum after converging with the second branch.
It can also be additionally provided with the heater that goes into operation on the second hydrogenation material conveyance conduit, and the heater that goes into operation
Positioned at the downstream that the tube side of the heat exchanger exports, to facilitate the heating needs that go into operation.
It is preferred that the heater that goes into operation is steam heater, steam in official website is utilized to facilitate, and hygiene.
In above-mentioned each scheme, the preferably described heat exchanger may include shell, and the top of the shell is exported equipped with tube side, institute
The bottom for stating shell is equipped with tube-side inlet, and the top of the shell is equipped with shell side inlet, and the lower part of the shell goes out equipped with shell side
Mouthful；
The interior intracavitary of the shell is equipped with heat exchanger tube, axis direction screw arrangement of the heat exchanger tube along the shell.
Core cylinder is equipped in the shell, the heat exchanger tube is wrapped on the core cylinder.
Use the pyrolysis gasoline hydrogenation method of above-mentioned pyrolysis gasoline hydrogenation device, it is characterised in that include the following steps：
After first burst of hydrogenating materials that temperature is 60~70 DEG C, pressure is 3.0~3.5MPa are mixed with first strand of recycle hydrogen
Formed temperature be 60~70 DEG C, the incoming mixture that pressure is 3.0~3.5MPa, be preheated to 80~90 into the preheater 3
DEG C, 2.9~3.4MPa, subsequently into the heat exchanger with from the hydrogenation reactor first burst of reaction product exchange heat
Afterwards, it is mixed with second burst of hydrogenating materials, the reaction raw materials that temperature is 230~250 DEG C, pressure is 2.8~3.3MPa is formed, from top
Portion enters in the hydrogenation reactor, and second strand of recycle hydrogen enters from middle part in the hydrogenation reactor, and it is anti-to carry out catalytic hydrogenation
It answers；Control that the reaction temperature in the hydrogenation reactor is 230~290 DEG C, pressure is 2.8~3.3MPa；
The volume ratio for controlling first strand of recycle hydrogen and first burst of hydrogenating materials is 300~600Nm3/m3；
First burst of reaction product temperature is 270~290 DEG C, pressure is 2.6~3.1MPa, is changed in the heat exchanger
Heat is discharged from the shell-side outlet of the heat exchanger to 100~120 DEG C, 2.5~3.0MPa, is with temperature in the second branch
270~290 DEG C, after second burst of reaction product that pressure is 2.6~3.1MPa mixing, send to the hydrogenation products knockout drum and carry out
Gas-liquid separation, gas phase and liquid phase after separation are discharged from the top and bottom of the hydrogenation products knockout drum respectively, send to downstream
Equipment.
Alternatively, using the pyrolysis gasoline hydrogenation method of above-mentioned pyrolysis gasoline hydrogenation device, it is characterised in that including following steps
Suddenly：
When going into operation, temperature is 60~70 DEG C, pressure is 3.0~3.5MPa first burst of hydrogenating materials and first strand of recycle hydrogen
After mixing formed temperature be 60~70 DEG C, the incoming mixture that pressure is 3.0~3.5MPa, be preheated to 80 into the preheater
~90 DEG C, 2.9~3.4MPa enter described open then via the tube side of the heat exchanger, after being mixed with second burst of hydrogenating materials
Work heater is heated to 230~250 DEG C, after 2.8~3.3MPa, enters in the hydrogenation reactor from top, carries out plus hydrogen is anti-
It answers；
When by steam supplementary heating, after reaction system is warming up to reaction temperature, go into operation heater described in closing；
At this point, first burst of hydrogenating materials that temperature is 60~70 DEG C, pressure is 3.0~3.5MPa are mixed with first strand of recycle hydrogen
Formed after conjunction temperature be 60~70 DEG C, the incoming mixture that pressure is 3.0~3.5MPa, be preheated to 80 into the preheater~
90 DEG C, 2.9~3.4MPa exchange heat subsequently into the heat exchanger with first burst of reaction product from the hydrogenation reactor
Afterwards, it is mixed with second burst of hydrogenating materials, the reaction raw materials that temperature is 230~250 DEG C, pressure is 2.8~3.3MPa is formed, from top
Portion enters in the hydrogenation reactor, and second strand of recycle hydrogen enters from middle part in the hydrogenation reactor, carries out hydrogenation reaction；Control
Make the reaction temperature in the hydrogenation reactor is 230~290 DEG C, pressure is 2.8~3.3MPa；
First burst of reaction product temperature is 270~290 DEG C, pressure is 2.6~3.1MPa, is changed in the heat exchanger
Heat is discharged from the shell-side outlet of the heat exchanger 2 to 100~120 DEG C, 2.5~3.0MPa, is with temperature in the second branch
270~290 DEG C, after second burst of reaction product that pressure is 2.6~3.1MPa mixing, send to the hydrogenation products knockout drum and carry out
Gas-liquid separation, gas phase and liquid phase after separation are discharged from the top and bottom of the hydrogenation products knockout drum respectively, send to downstream
Equipment.
The middle pressure steam or temperature that the heat source of the heater that goes into operation is preferably 340~380 DEG C, pressure is 3.5~4.0MPa
The high steam that degree is 440~480 DEG C, pressure is 9.5MPa.
Compared with prior art, pyrolysis gasoline hydrogenation device and method of hydrotreating provided by the utility model use plus hydrogen produces
Object is as heat transferring medium, and the structure by improving heat exchanger, and the heat exchange that more heat exchangers can be reached with a heat exchanger is imitated
Fruit greatly reduces low equipment investment, piping quantity and installation area；It eliminates and must be equipped in the prior art simultaneously
Charging heating furnace, reduce plant energy consumption, can reduce by 150~200kW by 700,000 tons/year of pyrolysis gasoline hydrogenation plant energy consumptions,
Energy conservation and consumption reduction effects are notable.Using the steam heater substitution heating furnace that goes into operation in preferred embodiment, energy consumption is further decreased, is steamed simultaneously
Vapour avoids furnace exhaust and discharges problem not up to standard, improve the device feature of environmental protection as clean energy resource.
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, which includes：
Hydrogenation reactor 1 is conventional pyrolysis gasoline second-stage hydrogenation reactor, and the interior hydrogenation reaction occurred is also conventional
Reaction.The top of hydrogenation reactor is equipped with first material entrance 11, and middle part is equipped with second material entrance 12, and bottom goes out equipped with material
Mouth 13.
Second circulation hydrogen conveyance conduit 64 connects the second material entrance 12 of the hydrogenation reactor 1.
Material outlet 13 is separately connected the first branch 15 and the second branch 14.
Heat exchanger, there are three, including heat exchanger 2, preheater 3 and the heater 4 that goes into operation.
Wherein, heat exchanger 2 includes shell 21, and the top of the shell 21 is equipped with tube side and exports 22, the bottom of the shell 21
Portion is equipped with tube-side inlet 23, and the top of the shell is equipped with shell side inlet 24, and the lower part of the shell 21 is equipped with shell-side outlet 25；
The interior intracavitary of the shell 21 is equipped with core cylinder 51 along the axis direction of shell, and the heat exchanger tube 5 is spirally wound on core
On cylinder 51, also, the outlet tube side outlet of heat exchanger tube 5, the entrance communicating pipe journey entrance of heat exchanger tube.
The second hydrogenation material conveyance conduit 62 of tube side outlet connection of heat exchanger 2.
The first branch 15 of the shell side inlet connection hydrogenation reaction of heat exchanger 2, the shell-side outlet and the second branch of heat exchanger 2
14 converge after connection hydrogenation products knockout drum 8 material inlet.
Preheater 3, for being preheated to first strand plus the incoming mixture of hydrogen charging and first strand of recycle hydrogen, setting exists
The upstream of heat exchanger 2, can select as needed it is in the prior art any one.
The tube-side inlet of preheater 3 connects the first hydrogenation material conveyance conduit 61 and first circulation hydrogen conveyance conduit 63, in advance
The tube-side inlet of the tube side outlet connection heat exchanger 2 of hot device 3；The second hydrogenation material conveyance conduit 62 connects hydrogenation reactor
1 first material entrance 11.
Go into operation heater 4, for heating the reaction raw materials entered in hydrogenation reactor when going into operation.The present embodiment is using steaming
Vapour heater；Go into operation heater 4 tube-side inlet connect the second hydrogenation material conveyance conduit 62, and positioned at heat exchanger tube pass export
Downstream, the heater 4 that goes into operation tube side outlet connection hydrogenation reactor first material entrance 11.
Pyrolysis gasoline hydrogenation method, includes the following steps：
When going into operation, product of the drippolene from naphtha pyrolysis ethylene unit after one-stage hydrogenation should as add
Hydrogen feedstock is mainly organized as C6~C8 fractions, wherein unsaturated monoolefine accounts for 10~20% (mass fractions), sulfur content 50~
200ppm, shape after first burst of hydrogenating materials that temperature is 60~70 DEG C, pressure is 3.0~3.5MPa are mixed with first strand of recycle hydrogen
At the incoming mixture that temperature is 60~70 DEG C, pressure is 3.0~3.5MPa, into the preheater 3 be preheated to 80~90 DEG C,
2.9~3.4MPa enters the heating that goes into operation then via the tube side of the heat exchanger 2, after being mixed with second burst of hydrogenating materials
Device 4, with temperature is 340~380 DEG C, pressure is 3.5~4.0MPa middle pressure steam or temperature be 440~480 DEG C, pressure is
9.5MPa high steams exchange heat, and are heated to 230~250 DEG C, after 2.8~3.3MPa, enter the hydrogenation reactor 1 from top
It is interior, carry out hydrogenation reaction；
When the heater 4 that by steam supplementary heating, goes into operation after reaction system is warming up to reaction temperature, described in closing；
At this point, first burst of hydrogenating materials that temperature is 60~70 DEG C, pressure is 3.0~3.5MPa are mixed with first strand of recycle hydrogen
After conjunction formed temperature be 60~70 DEG C, the incoming mixture that pressure is 3.0~3.5MPa, be preheated to 80 into the preheater 3
~90 DEG C, 2.9~3.4MPa, subsequently into the heat exchanger 2 with first burst of reaction product from the hydrogenation reactor 1
It after heat exchange, is mixed with second burst of hydrogenating materials, forms 230~250 DEG C, the reaction raw materials of 2.8~3.3MPa, enter institute from top
It states in hydrogenation reactor 1, second strand of recycle hydrogen enters from middle part in hydrogenation reactor 1 via second circulation hydrogen conveyance conduit 64,
Carry out hydrogenation reaction；
The volume ratio for controlling first strand of recycle hydrogen and first burst of hydrogenating materials is 300~600Nm3/m3。
Second burst of hydrogenating materials is primarily used to control into the temperature of the reaction raw materials of hydrogenation reactor, and dosage is to adjust
The temperature of section into the reaction raw materials of hydrogenation reactor, which is 230~250 DEG C, to be advisable；
The effect of second strand of recycle hydrogen is for adjusting the reaction temperature in hydrogenation reactor, and dosage is to control described add
Reaction temperature in hydrogen reactor is 230~290 DEG C, pressure is 2.8~3.3MPa；
First burst of reaction product temperature is 270~290 DEG C, pressure is 2.6~3.1MPa, in the heat exchanger 2
Heat exchange is discharged to 100~120 DEG C, 2.5~3.0MPa from the shell-side outlet of the heat exchanger 2, with temperature in the second branch 14
Degree is 270~290 DEG C, after the mixing of second burst of reaction product that pressure is 2.6~3.1MPa, formed 100~120 DEG C, 2.5~
The reaction product of 3.0MPa sends to the hydrogenation products knockout drum 8 and carries out gas-liquid separation, the gas phase and liquid phase after separation respectively from
The top and bottom of the hydrogenation products knockout drum 8 are discharged.
Main group of the gas phase that hydrogenation products knockout drum 8 is discharged becomes H2、H2S、NH3With C4- (C4 alkane below)；It send
Remove follow-up equipment.
The H that it hydrogasoline (C6~C8 fractions) that main group of the liquid phase of discharge, which becomes, is dissolved in gasoline2S、NH3Deng former
Alkene in material is all saturated, sulphur concentration ＜ 1ppm；Fractionation process is sent to from knockout drum bottom.
Claims (5)
1. a kind of pyrolysis gasoline hydrogenation device, including hydrogenation reactor (1) and heat exchanger, it is characterised in that：
The heat exchanger includes heat exchanger (2) and preheater (3)；
Wherein, the tube-side inlet of the heat exchanger (2) connects the tube side outlet of the preheater (3)；
The tube-side inlet of the preheater (3) connects the first hydrogenation material conveyance conduit (61) and first circulation hydrogen conveyance conduit
(63), the second hydrogenation material conveyance conduit (62) of tube side outlet connection of the heat exchanger (2), the second hydrogenation material conveying
Pipeline (62) connects the first material entrance (11) of hydrogenation reactor (1), and second circulation hydrogen conveyance conduit (64) connection is described to be added
The second material entrance (12) of hydrogen reactor (1), material outlet (13) the connection first branch (15) of the hydrogenation reactor (1)
With the second branch (14)；Wherein the first branch (15) connects the shell side inlet of the heat exchanger (2), and the shell side of the heat exchanger goes out
The material inlet of connection hydrogenation products knockout drum (8) after mouth converges with the second branch (14).
2. pyrolysis gasoline hydrogenation device according to claim 1, it is characterised in that the second hydrogenation material conveyance conduit
(62) heater that goes into operation (4) is additionally provided on, and the heater that goes into operation (4) is located under the tube side outlet of the heat exchanger
Trip.
3. pyrolysis gasoline hydrogenation device according to claim 2, it is characterised in that the heater that goes into operation (4) adds for steam
Hot device.
4. the pyrolysis gasoline hydrogenation device according to claims 1 to 3 any claim, it is characterised in that the heat exchanger
(2) include shell (21), the top of the shell (21) is equipped with tube side and exports (22), and the bottom of the shell (21) is equipped with tube side
The top of entrance (23), the shell is equipped with shell side inlet (24), and the lower part of the shell (21) is equipped with shell-side outlet (25)；
The interior intracavitary of the shell (21) is equipped with heat exchanger tube (5), axis direction spiral shell of the heat exchanger tube (5) along the shell (21)
Rotation arrangement.
5. pyrolysis gasoline hydrogenation device according to claim 4, it is characterised in that be equipped with core cylinder in the shell (21)
(51), the heat exchanger tube (5) is wrapped on the core cylinder (51).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721565838.0U CN207608526U (en) | 2017-11-21 | 2017-11-21 | pyrolysis gasoline hydrogenation device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721565838.0U CN207608526U (en) | 2017-11-21 | 2017-11-21 | pyrolysis gasoline hydrogenation device |
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| Publication Number | Publication Date |
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| CN207608526U true CN207608526U (en) | 2018-07-13 |
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ID=62795718
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| CN201721565838.0U Active CN207608526U (en) | 2017-11-21 | 2017-11-21 | pyrolysis gasoline hydrogenation device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107937022A (en) * | 2017-11-21 | 2018-04-20 | 宁波东鼎石化装备有限公司 | Pyrolysis gasoline hydrogenation device and method |
-
2017
- 2017-11-21 CN CN201721565838.0U patent/CN207608526U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107937022A (en) * | 2017-11-21 | 2018-04-20 | 宁波东鼎石化装备有限公司 | Pyrolysis gasoline hydrogenation device and method |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20190625 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. |
|
| TR01 | Transfer of patent right | ||
| 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. |
|
| CP01 | Change in the name or title of a patent holder |