CN205473599U - Retrieve device of cold volume of contact again of reforming - Google Patents
Retrieve device of cold volume of contact again of reforming Download PDFInfo
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- CN205473599U CN205473599U CN201521026846.9U CN201521026846U CN205473599U CN 205473599 U CN205473599 U CN 205473599U CN 201521026846 U CN201521026846 U CN 201521026846U CN 205473599 U CN205473599 U CN 205473599U
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- heat exchanger
- contact tank
- tank
- separatory
- contact
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model relates to a retrieve device of cold volume of contact again of reforming, it includes the reforming reaction oil -gas separation unit and fractionation unit that connects gradually, wherein, reforming reaction oil -gas separation unit including the knockout drum that connects gradually, again contact pot take one's place calorimeter, at the bottom of contact pot heat exchanger, refrigerating unit and contact pot more again, divide export of fluid reservoir bottom and contact pot again to take one's place the calorimeter and link to each other, again contact pot take one's place the calorimeter in proper order with contact pot again at the bottom of heat exchanger, refrigerating unit and again the contact pot feed inlet link to each other, again at the bottom of the contact pot heat exchanger with distillate fractionally the unit feed inlet and link to each other. The utility model discloses an after newly -increased top gas of contact pot again or the dechlorination reformation hydrogen with the heat transfer of fluid reservoir liquid phase divides, perhaps with the mixture after the gas -liquid two -phase heat transfer, the cold volume that all can fully retrieve reformation hydrogen effectively reduces refrigerating unit's system cooling load, reduce refrigeration power consumption 20 30%, have obvious energy -conserving effect.
Description
Technical field
This utility model relates to oil-refining chemical production system, especially relates to a kind of recovery reformation and contacts cold again
Device.
Background technology
Reformer belongs to oil refining secondary operations device, mainly with low-octane straight-run naphtha, hydrogenation stone
, under catalyst and certain pressure, temperature conditions, there is reforming reaction, produce Gaoxin in the raw materials such as cerebrol
The Reformed Gasoline of alkane value, and by-product hydrogen, Reformed Gasoline can be as aroamtic hydrocarbon raw material, or as gasoline mediation group
Point.
The current reformer technological process of production includes pretreatment of raw material, reforming reaction, Oil-gas Separation, product
Product fractional distillation and catalyst five parts of regeneration.Wherein raw material pretreatment process flow process is usually: reforming reaction is produced
Thing, after heat exchange, cooling, enters reforming reaction product separator (separatory tank), carries out gas-liquid separation.Separatory
Tank gas phase divides two-way, and wherein a road is after circulating hydrogen compressor compresses, and returns reforming reaction system as recycle hydrogen
System；Another road is through hydrogen booster supercharging, after air cooler cools down, with the separatory tank after pump pressurizes
Liquid phase mixes again.After liquid heat exchange at the bottom of mixed gas-liquid two-phase and again contact tank, then freeze through refrigeration unit,
Entering contact tank again and carry out gas-liquid separation, tank deck gas phase is attached most importance to whole hydrogen, dechlorinated after enter hydrogen upgrading system
Or hydrogen pipe network；Again liquid at the bottom of contact tank successively with contact charging, fractionating column base oil heat exchange again after, enter fractional distillation
Tower separates further, as Reformed Gasoline or aroamtic hydrocarbon raw material after fractionating column base oil and charging heat exchange.
It is relatively low that above-mentioned reformation contacts tank deck reformation hydrogen temperature again, the unrecovered utilization of cold, to hydrogen upgrading system,
Need again heating, there is the phenomenon of energy waste.
CN202297110U discloses a kind of hydrogen cold recycling system for continuous reforming device, including continuously
Hydrogen in reformer extracts and dechlorination unit and liquefied gas cooling unit, extracts and dechlorination at described hydrogen
Heat exchanger is set up, by the low temperature hydrogen from ammonia device for cooling and from surely between unit and liquefied gas cooling unit
Determine column overhead volatile matter heat exchange, improve hydrogen product temperature, reduce the temperature of fractionator overhead volatile matter simultaneously,
Fully recovering liquid hydrocarbon.
Above method is to design, the most also from the angle improving hydrogen product temperature and increase liquid hydrocarbon
The cold of reformation hydrogen can be reclaimed, but this flow process there is also high-quality low problem, and hydrogen-cooled amount of reforming fails to fill
Divide and reclaim.Therefore, the most fully reclaiming the cold of reformation hydrogen, the load reducing refrigeration unit has become current
Problem demanding prompt solution.
Utility model content
For solving the problems referred to above of prior art, the purpose of this utility model there are provided a kind of new recovery
Reforming and contact the device of cold again, this utility model can fully reclaim the cold of reformation hydrogen, reduce refrigeration machine
The cooling load of group, reduces power consumption of refrigerating, has obvious energy-saving effect.
For reaching this purpose, this utility model have employed techniques below scheme:
This utility model provide a kind of reclaim to reform contact the device of cold again, it includes the weight being sequentially connected with
Whole reaction oil gas separative element and fractionation unit, wherein, described reforming reaction Oil-gas Separation unit includes successively
The knockout drum that connects, again heat exchanger at the bottom of contact tank top heat exchanger, again contact tank, refrigeration unit and contact tank again,
Separatory pot bottom outlet be connected with contact tank top heat exchanger again, then contact tank top heat exchanger successively with contact tank again
End heat exchanger, refrigeration unit and again contact tank charging aperture be connected, then heat exchanger at the bottom of contact tank and fractionation unit
Charging aperture is connected.
In this utility model, described reforming reaction Oil-gas Separation unit also includes reformation input and output material heat exchanger, sky
The tank bottoms pump of Gas Cooler, water recirculator, separatory, circulating hydrogen compressor, hydrogen booster and air are cold
But device, reformation input and output material heat exchanger and air cooler and water recirculator and separatory tank entrance phase successively
Even, the outlet of separatory tank top is connected with circulating hydrogen compressor and hydrogen booster respectively, and hydrogen booster exports
Being connected with air cooler entrance, separatory pot bottom exports through the tank bottoms pump of separatory and contact tank top heat exchanger phase again
Even.
In this utility model, described fractionation unit includes fractionating column feed exchanger and fractionating column, wherein, institute
State again heat exchanger at the bottom of contact tank to be connected with fractionating column feed exchanger and fractionating column charging aperture successively.
Specifically, the device that recovery reformation described in the utility model contacts cold again includes:
Reformation input and output material heat exchanger, air cooler, water recirculator, separatory tank, the tank bottoms pump of separatory,
Change at the bottom of circulating hydrogen compressor, hydrogen booster, air cooler, again contact tank top heat exchanger, again contact tank
Hot device, refrigeration unit, again contact tank, fractionating column feed exchanger and fractionating column, wherein, reformation input and output material
Heat exchanger and air cooler and water recirculator and separatory tank entrance are sequentially connected, and separatory tank top goes out
Mouth is connected with circulating hydrogen compressor and hydrogen booster respectively, hydrogen booster outlet and air cooler entrance
Being connected, the outlet of separatory pot bottom is connected with contact tank top heat exchanger again through the tank bottoms pump of separatory, then contact tank is taken one's place
Hot device successively with heat exchanger at the bottom of contact tank again, refrigeration unit and again contact tank charging aperture be connected, then contact tank
End heat exchanger is connected with fractionating column feed exchanger and fractionating column charging aperture successively.
This utility model passes through reformation hydrogen and separatory tank liquid phase heat exchange after newly-increased contact tank top gas again or dechlorination, or
Person and mixed gas-liquid two-phase heat exchange, all can fully reclaim the cold of reformation hydrogen, effectively reduce refrigeration machine
The cooling load of group, reduces power consumption of refrigerating 20-30%, has obvious energy-saving effect.
This utility model by using tank deck gas phase entering before hydrogen upgrading system, first with contact charging again
Cold is reclaimed in heat exchange, and it can preferably reclaim the cold of reformation hydrogen, have good energy-saving effect.
Device described in the utility model is utilized to carry out reclaiming reforming and contact the method for cold again and specifically include following
Step: reforming reaction product, after heat exchange, cooling, enters separatory tank, carries out gas-liquid separation；Separatory tank gas
Dividing two-way mutually, wherein a road is after circulating hydrogen compressor compresses, and returns reforming reaction system as recycle hydrogen；
Another road is through hydrogen booster supercharging, after air cooler cools down, then with pressurized and cooling after separatory
Tank liquid-phase mixing；Mixed gas-liquid two-phase enters back into heat exchanger at the bottom of contact tank again, with contact tank again at the bottom of liquid change
Heat, after freeze through refrigeration unit, enter again contact tank and carry out gas-liquid separation；Contact tank top gas is attached most importance to mutually again
Whole hydrogen, after first reclaiming cold with separatory tank liquid phase heat exchange, more dechlorinated after, enter hydrogen upgrading system or hydrogen
Gas pipe network；Again liquid phase at the bottom of contact tank successively with contact charging, fractionating column base oil heat exchange again, enter fractionating column enter
Row separates further, as Reformed Gasoline or aroamtic hydrocarbon raw material after fractionating column base oil and charging heat exchange.
Compared with prior art, this utility model at least has the advantages that
The recovery reformation that this utility model provides contacts the cold of the method and device recyclable reformation hydrogen of cold again
Amount, reduces the cooling load of refrigeration unit, reduces power consumption of refrigerating 20-30%, has good energy-saving effect.
Accompanying drawing explanation
Fig. 1 is the reformation hydrogen-cooled amount recovery process figure of this utility model embodiment 1；
Fig. 2 is the reformation hydrogen-cooled amount recovery process figure of this utility model embodiment 2；
Wherein, 1-reformation input and output material heat exchanger, 2-air cooler, 3-water recirculator, 4-separatory tank,
The tank bottoms pump of 5-separatory, 6-circulating hydrogen compressor, 7-hydrogen booster, 8-air cooler, 9-contacts tank deck again
Heat exchanger, heat exchanger at the bottom of 10-contact tank again, 11-refrigeration unit, 12-contact tank again, the charging of 13-fractionating column is changed
Hot device, 14-fractionating column.
Detailed description of the invention
For ease of understanding this utility model, it is as follows that this utility model enumerates embodiment.Those skilled in the art should
This understands, the only help of described embodiment understands this utility model, is not construed as tool of the present utility model
Body limits.
Embodiment 1
As a example by 1,000,000 tons/year of reformers of certain oil plant, illustrate that the present invention reforms and contact cold recovery dress again
Put.
The hydrogen-cooled amount recovery process flow process as it is shown in figure 1, the one described in the present embodiment is reformed, concrete steps are such as
Under:
Reforming reaction product (493 DEG C, 0.32MPag) from reforming reactor sequentially enters reformation input and output material
Heat exchanger 1 heat exchange is to 105 DEG C, then is cooled to 40 DEG C through air cooler 2 and water recirculator 3, enters
Enter separatory tank 4.
Gas phase in separatory tank 4 divides two-way, and a road is compressed through circulating hydrogen compressor 6, and another road increases through hydrogen
After press 7 is pressurized to 2.2MPa, enter air cooler 8 cool down, with through separatory tank bottoms pump 5 pressurize after
The tank bottoms liquid phase of separatory mixes again.Mixed gas-liquid two-phase enters contact tank top heat exchanger 9 again, and contacts again
Head space gas heat exchange, enters back into liquid heat exchange at the bottom of heat exchanger 10, with contact tank again at the bottom of contact tank again, after through refrigeration
Unit refrigeration 11 is cooled to 4 DEG C, enters contact tank 12 again and carries out gas-liquid separation, then contact tank 12 top gas phase
For reformation hydrogen, first with contact charging heat exchange recovery cold again after, more dechlorinated after, entrance hydrogen upgrading system；
Heat exchanger 10, fractionating column feed exchanger 13 at the bottom of liquid phase at the bottom of contact tank sequentially enters contact tank again again, successively with
Contact tank charging again, fractionating column base oil heat exchange, enter fractionating column 14 and separate further, fractionating column base oil
With charging heat exchange after as Reformed Gasoline or aroamtic hydrocarbon raw material.
Wherein used reclaim reform contact again the device of cold specifically include that reformation input and output material heat exchanger 1,
Air cooler 2, water recirculator 3, separatory tank 4, the tank bottoms pump of separatory 5, circulating hydrogen compressor 6, hydrogen
Heat exchanger 10, refrigeration at the bottom of gas supercharger 7, air cooler 8, again contact tank top heat exchanger 9, again contact tank
Unit 11, again contact tank 12, fractionating column feed exchanger 13 and fractionating column 14, wherein, reformation input and output material
Heat exchanger 1 and air cooler 2 and water recirculator 3 and separatory tank 4 entrance are sequentially connected, separatory
Tank 4 top exit is connected with circulating hydrogen compressor 6 and hydrogen booster 7 respectively, and hydrogen booster 7 exports
Being connected with air cooler 8 entrance, the outlet of separatory pot bottom takes one's place heat through the tank bottoms pump of separatory 5 with contact tank again
Device 9 is connected, then contact tank top heat exchanger 9 successively with contact tank again at the bottom of heat exchanger 10, refrigeration unit 11 and
Again contact tank 12 charging aperture be connected, then heat exchanger 10 at the bottom of contact tank successively with fractionating column 14 feed exchanger and
Fractionating column 14 charging aperture is connected.
Embodiment 2
As in figure 2 it is shown, a kind of reformation hydrogen cold recovery work described in the present embodiment as different from Example 1
Process flow, specifically comprises the following steps that
Reforming reaction product (493 DEG C, 0.32MPag) from reforming reactor sequentially enters reformation input and output material
Heat exchanger 1 heat exchange is to 105 DEG C, then is cooled to 40 DEG C through air cooler 2 and water recirculator 3, enters
Enter separatory tank 4.Gas phase in separatory tank 4 divides two-way, and a road is compressed through circulating hydrogen compressor 6, another road warp
After hydrogen booster 7 is pressurized to 2.2MPa, enters air cooler 8 and cool down, add with through cold high score liquid pump 5
The tank bottoms oil of separatory after pressure mixes again.First and contact tank top gas heat exchange again before separatory tank bottoms oil mixing, mixed
Gas-liquid two-phase after conjunction enters liquid heat exchange at the bottom of heat exchanger 10, with contact tank again at the bottom of contact tank again, after through refrigeration
Unit refrigeration 11 is cooled to 4 DEG C, enters contact tank 12 again and carries out gas-liquid separation, and tank deck gas phase is attached most importance to whole hydrogen,
Enter contact tank top heat exchanger 9 again, after cold is reclaimed in oil tank bottoms with separatory heat exchange, more dechlorinated after enter hydrogen
Upgrading system；Heat exchanger 10, fractionating column feed exchanger 13 at the bottom of contact tank base oil sequentially enters contact tank again again,
Successively with the charging of contact tank again, fractionating column base oil heat exchange, enter fractionating column 14 and separate further, fractional distillation
As Reformed Gasoline or aroamtic hydrocarbon raw material after tower base oil and charging heat exchange.
Wherein used reclaim reform contact again the device of cold specifically include that reformation input and output material heat exchanger 1,
Air cooler 2, water recirculator 3, separatory tank 4, the tank bottoms pump of separatory 5, circulating hydrogen compressor 6, hydrogen
Heat exchanger 10, refrigeration at the bottom of gas supercharger 7, air cooler 8, again contact tank top heat exchanger 9, again contact tank
Unit 11, again contact tank 12, fractionating column feed exchanger 13 and fractionating column 14, wherein, reformation input and output material
Heat exchanger 1 and air cooler 2 and water recirculator 3 and separatory tank 4 entrance are sequentially connected, separatory
Tank 4 top exit is connected with circulating hydrogen compressor 6 and hydrogen booster 7 respectively, and hydrogen booster 7 exports
Being connected with air cooler 8 entrance, the outlet of separatory pot bottom takes one's place heat through the tank bottoms pump of separatory 5 with contact tank again
Device 9 is connected, then contact tank top heat exchanger 9 successively with contact tank again at the bottom of heat exchanger 10, refrigeration unit 11 and
Again contact tank 12 charging aperture be connected, then heat exchanger 10 at the bottom of contact tank successively with fractionating column feed exchanger and divide
Evaporate tower charging aperture to be connected.
The technique using the present invention, the cooling load of refrigeration unit is reduced to 2150kW from 2800kW, reduces
23.2%, energy-saving effect is obvious.
Applicant states, by above-described embodiment, this utility model illustrates that detailed process of the present utility model sets
Standby and technological process, but this utility model is not limited to above-mentioned detailed process equipment and technological process, the most not
Mean that this utility model has to rely on above-mentioned detailed process equipment and technological process could be implemented.Affiliated technology
The technical staff in field is it will be clearly understood that to any improvement of the present utility model, each former to this utility model product
The equivalence of material is replaced and the interpolation of auxiliary element, concrete way choice etc., all falls within guarantor of the present utility model
Within the scope of protecting scope and disclosure.
Claims (4)
1. one kind is reclaimed to reform and contacts the device of cold again, it is characterised in that it includes the reformation being sequentially connected with
Reaction oil gas separative element and fractionation unit, wherein, described reforming reaction Oil-gas Separation unit includes connecting successively
Heat exchanger at the bottom of the knockout drum that connects, again contact tank top heat exchanger, again contact tank, refrigeration unit and contact tank again,
Separatory pot bottom outlet be connected with contact tank top heat exchanger again, then contact tank top heat exchanger successively with contact tank again
End heat exchanger, refrigeration unit and again contact tank charging aperture be connected, then heat exchanger at the bottom of contact tank and fractionation unit
Charging aperture is connected.
Device the most according to claim 1, it is characterised in that described reforming reaction Oil-gas Separation unit
Also include reformation input and output material heat exchanger, air cooler, water recirculator, the tank bottoms pump of separatory, recycle hydrogen
Compressor, hydrogen booster and air cooler, reformation input and output material heat exchanger and air cooler and recirculated water
Cooler and separatory tank entrance are sequentially connected, separatory tank top outlet respectively with circulating hydrogen compressor and hydrogen
Supercharger is connected, and hydrogen booster outlet is connected with air cooler entrance, and separatory pot bottom exports through separatory
Tank bottoms pump is connected with contact tank top heat exchanger again.
Device the most according to claim 1, it is characterised in that described fractionation unit includes that fractionating column enters
Material heat exchanger and fractionating column, wherein, heat exchanger at the bottom of described contact tank more successively with fractionating column feed exchanger and
Fractionating column charging aperture is connected.
Device the most according to claim 1, it is characterised in that described device includes:
Reformation input and output material heat exchanger, air cooler, water recirculator, separatory tank, the tank bottoms pump of separatory,
Change at the bottom of circulating hydrogen compressor, hydrogen booster, air cooler, again contact tank top heat exchanger, again contact tank
Hot device, refrigeration unit, again contact tank, fractionating column feed exchanger and fractionating column, wherein, reformation input and output material
Heat exchanger and air cooler and water recirculator and separatory tank entrance are sequentially connected, and separatory tank top goes out
Mouth is connected with circulating hydrogen compressor and hydrogen booster respectively, hydrogen booster outlet and air cooler entrance
Being connected, the outlet of separatory pot bottom is connected with contact tank top heat exchanger again through the tank bottoms pump of separatory, then contact tank is taken one's place
Hot device successively with heat exchanger at the bottom of contact tank again, refrigeration unit and again contact tank charging aperture be connected, then contact tank
End heat exchanger is connected with fractionating column feed exchanger and fractionating column charging aperture successively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521026846.9U CN205473599U (en) | 2015-12-10 | 2015-12-10 | Retrieve device of cold volume of contact again of reforming |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521026846.9U CN205473599U (en) | 2015-12-10 | 2015-12-10 | Retrieve device of cold volume of contact again of reforming |
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| Publication Number | Publication Date |
|---|---|
| CN205473599U true CN205473599U (en) | 2016-08-17 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201521026846.9U Expired - Fee Related CN205473599U (en) | 2015-12-10 | 2015-12-10 | Retrieve device of cold volume of contact again of reforming |
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| CN (1) | CN205473599U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105441118A (en) * | 2015-12-10 | 2016-03-30 | 上海优华***集成技术股份有限公司 | Method and apparatus for recovering cold quantity of reforming and re-contacting |
| WO2019231753A1 (en) * | 2018-06-01 | 2019-12-05 | Chevron Phillips Chemical Company Lp | Method of separating and recycling hydrogen in an aromatization process |
-
2015
- 2015-12-10 CN CN201521026846.9U patent/CN205473599U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105441118A (en) * | 2015-12-10 | 2016-03-30 | 上海优华***集成技术股份有限公司 | Method and apparatus for recovering cold quantity of reforming and re-contacting |
| WO2019231753A1 (en) * | 2018-06-01 | 2019-12-05 | Chevron Phillips Chemical Company Lp | Method of separating and recycling hydrogen in an aromatization process |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20160817 Termination date: 20211210 |