CN208959573U - A kind of oil refinery dry gas recovery system - Google Patents
A kind of oil refinery dry gas recovery system Download PDFInfo
- Publication number
- CN208959573U CN208959573U CN201821397310.1U CN201821397310U CN208959573U CN 208959573 U CN208959573 U CN 208959573U CN 201821397310 U CN201821397310 U CN 201821397310U CN 208959573 U CN208959573 U CN 208959573U
- Authority
- CN
- China
- Prior art keywords
- outlet
- desorber
- connect
- oil refinery
- absorption tower
- 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.)
- Active
Links
Abstract
The utility model relates to oil refinery dry gas process fields, specifically disclose a kind of oil refinery dry gas recovery system, including sequentially connected residue gas compressor, dehydration demercuration bed, ice chest, absorption tower, flash tank and desorber；The feed(raw material)inlet of the residue gas compressor is connect with the raw material conveying device for supplying oil refinery dry gas, the tower top gas outlet of the desorber connects product conveying device, the first entrance of the product conveying device is connect with the desorber, and the second entrance of the product conveying device is connect with the ice chest；The gas outlet of the ice chest and the air inlet on absorption tower connect, and are additionally provided with the first coolant entrance and the first coolant outlet and the second coolant entrance and the second coolant outlet on the ice chest.Process system process flow disclosed by the utility model is simple and convenient to operate, low energy consumption, and all has the higher rate of recovery to ethane, ethylene, propane and propylene.
Description
Technical field
The utility model relates to oil refinery dry gas process fields, and in particular to a kind of oil refinery dry gas recovery system.
Background technique
Oil refinery dry gas is mainly derived from the crude distillation of petrochemical plant, catalytic cracking, petroleum coking, the stones such as is hydrocracked
Oily time processing or secondary processing process.Oil refinery dry gas is a kind of mixed gas, is rich in ethane, ethylene, propane in oil refinery dry gas
Equal two component of light hydrocarbons carbon or the components such as three component of carbon and hydrogen, methane and a small amount of impurity, wherein ethane and propylene are in agriculture
Medicine, medicine, fuel, coating, surfactant, resin etc. are widely used, and are the raw materials of numerous materials synthesis, and ethane and
Propane is therefore one of most important raw material during ethylene or production of propylene recycles value from oil refinery dry gas again
Higher lighter hydrocarbons are to increasing economic efficiency and environmental benefit is of great significance.
The method for recycling lighter hydrocarbons from oil refinery dry gas at present mainly has cryogenic separation method, middle cold oil absorption process, Separation by Complexation
Method or pressure swing adsorption method etc., wherein for pressure swing adsorption method because easy to operate, cost of investment is lower and of increasing concern.But
The pressure swing adsorption method used in the prior art recycles that the generally existing rate of recovery of light hydrocarbons is low, energy consumption is high from oil refinery dry gas
The problem of.
For example, Chinese patent literature CN101575254A discloses a kind of oil refinery dry gas recycling polymer grade ethylene technique, packet
It includes oil refinery dry gas compressed, remove sour gas, after the cooling that cleans, is sent into butane removing tower, which can eliminate because absorbing
Weight carbon four is easy to light dydrocarbon diene polymerization and brings the danger of explosion in the process, and simple process, cost of investment is low, and has higher
Recovery rate of ethylene, but it is lower to the rate of recovery of ethane, and can not effectively recycle C3 fraction, is not suitable for being rich in
The recycling of the oil refinery dry gas of C3 fraction.
Chinese patent literature CN104419464B discloses a kind of oil refinery dry gas recovery system and oil refinery dry gas recovery method,
The system comprises: compressor, absorption tower, desorber, expanding machine-cold box system, liquefaction cooler；Compressor connection absorbs
Tower, absorption tower tower reactor connect desorber, and desorber connects absorption tower top, connects expanding machine-cold box system, institute at the top of absorption tower
Stating expanding machine-cold box system includes ice chest, expanding machine, supercharger and flash tank, although the absorption system equipment is few, process letter
It is single, but other lighter hydrocarbons in addition to ethylene, the rate of recovery such as ethane, propylene, propane is lower, and process is complicated, energy
Source consumption is relatively high, invests relatively large.
In conclusion existing oil refinery dry gas recycling is recycled mainly for the ethylene in oil refinery dry gas, and it is right
In the rate of recovery needs further research for the ethane, propylene or propane for how improving higher-value, in addition, prior art is deposited
In the problem that energy consumption is high, the rate of recovery is low, process is complicated etc..
Utility model content
Therefore, the technical problem to be solved by the present invention is to overcome, the existing rate of recovery in the prior art is low, energy
The problem that consumption is high, technique applicability is limited, provides a kind of oil refinery dry gas recovery system, the recovery system technique stream of the utility model
Journey is simple and convenient to operate, low energy consumption, and all has the higher rate of recovery to ethane, ethylene, propane and propylene.
In order to solve the above-mentioned technical problem, the utility model provides a kind of oil refinery dry gas recovery system, including successively connects
Residue gas compressor, dehydration demercuration bed, ice chest, absorption tower, flash tank and the desorber connect；
Wherein, the feed(raw material)inlet of the residue gas compressor is connect with the raw material conveying device for supplying oil refinery dry gas, institute
State the tower top gas outlet connection product conveying device of desorber, the first entrance of the product conveying device and the desorber
The connection of tower top gas outlet, the second entrance of the product conveying device are connect with the ice chest；
The gas outlet of the ice chest and the air inlet on absorption tower connect, and are additionally provided on the ice chest for the first coolant flow
It passes to the first coolant entrance for recycling its cooling capacity and the first coolant outlet and is passed to for the second coolant flow and recycle its cooling capacity
The second coolant entrance and the second coolant outlet, the first coolant entrance of the ice chest and the tower top gas outlet on absorption tower
Connection, the second coolant entrance of the ice chest are connect with flash tank, and the second coolant outlet and product of the ice chest convey
The second entrance of device connects；
The inlet of the flash tank and the tower reactor liquid outlet on absorption tower connect, the tank deck gas outlet of the flash tank with it is cold
Second coolant entrance of case connects, and the tank bottom liquid outlet of the flash tank and the inlet of desorber connect.
It further include the poor of the tower reactor liquid outlet output of the rich solution and desorber for the tank bottom liquid outlet output for flash tank
Solvent carries out the poor rich liquid heat exchanger of heat exchange, and the rich solution entrance of the poor rich liquid heat exchanger and the tank bottom of the flash tank go out
The inlet of the connection of liquid mouth, the rich solution outlet of the poor rich liquid heat exchanger and desorber connects, the poor rich liquid heat exchanger it is poor
The connection of the tower reactor liquid outlet of colvent inlet and desorber, the inlet of the lean solvent outlet and absorption tower of the poor rich liquid heat exchanger
Connection.
It further include that the deoxidation for being connected to the residue gas compressor and being dehydrated between demercuration bed adds hydrogen bed, the deoxidation adds hydrogen bed
Air inlet connect the gas outlet of the residue gas compressor, the deoxidation adds the gas outlet of hydrogen bed to connect the air inlet of dehydration demercuration bed
Mouthful.
The absorption tower can perhaps the packed tower desorber can use plate column or filler using plate column
Tower.
When using plate column, the theoretical cam curve on the absorption tower is 20-30 block, the theoretical cam curve of the desorber
For 3-20 block.
The operating pressure on the absorption tower is 1.0~3.0MPa, and tower top temperature is 0~-30 DEG C.
The operating pressure of the desorber is 0.1~1.0MPa, and tower top temperature is 130~160 DEG C.
The air inlet on the absorption tower is located on the corresponding side wall of 2-5 block column plate of absorption tower from bottom to top, the suction
The inlet for receiving tower is located on the top-down 1st piece of corresponding side wall of column plate in absorption tower.
The inlet of the desorber is located on the corresponding side wall of the top-down 1-4 block column plate of desorber.
The absorption tower tower reactor and desorption tower reactor are provided with reboiler.
The adsorbent that the dehydration demercuration bed uses is in molecular sieve, active carbon, sulfur loading active carbon or active carbon of silver
It is a kind of or at least two mixture.
The utility model additionally provides a kind of oil refinery dry gas recovery method, includes the following steps:
Oil refinery dry gas, then will be rich after absorbent absorbs after compression boosting, deoxidation add hydrogen, dehydration demercuration, cool
The rich solution and fuel gas of three component of carbon containing two component and carbon separate, then rich solution is obtained to product gas and poor molten after desorbing
Agent；
Wherein, the absorbent is polyalcohol ether, and the polyalcohol ether has the structure as shown in formula (I)；
CxHy-(O-CH2-CH2)n-OCxHy(Ⅰ)；
Wherein, n=2-8, x=1y=3 or x=4y=9.
It further include cold recovery process, the cold absorption carries out simultaneously with the process of cooling, the cold recovery
Detailed process are as follows: before rich solution is through desorption procedure, rich solution is depressured rapidly and isolates part rich in two component of carbon and three groups of carbon
The product gas divided, it is cooling using the product gas and the fuel gas isolated through absorption process as the first coolant and second
Agent transfers out after cooling capacity therein is recycled in heat exchange with oil refinery dry gas respectively again simultaneously.
It further include heat exchanging process, the detailed process of the heat exchange are as follows: the lean solvent that will be generated first through desorption process
The rich solution generated as heat source and absorption process carries out heat exchange, is transported to desorption procedure, lean solvent conduct after rich solution heating
Absorbent is back to absorption step.
Oil refinery dry gas is boosted into 1.0-3.0MPa in the compression process.
The desorption procedure can be using steam, air or nitrogen as stripping gas.
The oil refinery dry gas be heavy oil catalytic cracking oil refinery dry gas, delayed coking oil refinery dry gas, desulfurization-hydrogenation oil refinery dry gas,
One of hydrogen manufacturing oil refinery dry gas and lighter hydrocarbons recovery oil refinery dry gas or at least two mixing oil refinery dry gas.
Technical solutions of the utility model have the advantages that
1. oil refinery dry gas recovery system provided by the utility model, by the setting of the enterprising port of ice chest and gas outlet and
The first coolant entrance for recycling its cooling capacity and the first coolant outlet are passed to for the first coolant flow on ice chest and confession is second cold
But agent is circulated to recycle the setting of the second coolant entrance and the second coolant outlet of its cooling capacity, wherein the first coolant enters
Mouth, the second coolant entrance and air inlet are de- with the tower top gas outlet on absorption tower, the tank deck gas outlet of flash tank and dehydration respectively
The gas outlet of mercury bed is connected, and enables through dehydration demercuration bed treated tower of the oil refinery dry gas in ice chest with absorption tower
The tank deck gas of top gas body and flash tank carries out heat exchange simultaneously, improves heat exchange efficiency, realizes simultaneously to storing up in two kinds of gases
The cooling capacity deposited is recycled, and is not only accelerated and is cooled to oil refinery dry gas, but also improves heat exchange uniformity and thermal energy benefit
With rate, so that it is not necessary that oil refinery dry gas can be cooled to 0 DEG C hereinafter, meeting absorption tower low temperature by additionally increase external cold source
Absorption process significantly reduces the energy consumption in oil refinery dry gas removal process to the temperature requirement of oil refinery dry gas；And this reality
Two tower absorption techniques, advantage also simple, easy to operate, stable with process flow are used with novel.
2. oil refinery dry gas recovery system provided by the utility model is located at the flash tank of tower reactor connection, energy by absorption tower
The absorption tower i.e. rich solution of tower reactor high pressure saturated liquid is enough set to reduce rapidly pressure, so that some hydrocarbon gasification in rich solution is transformed into gas
Body and separated from liquid, thus reduce carry out desorber rich solution flow, reduce the processing load of desorber, and then subtract
Required steam consumption when desorbing less, so that the energy consumption in oil refinery dry gas removal process is further decreased.
3. oil refinery dry gas recovery system provided by the utility model, rich solution entrance and institute by the poor rich liquid heat exchanger
The tank bottom liquid outlet connection of flash tank is stated, the rich solution outlet of the poor rich liquid heat exchanger and the inlet of desorber connect, described
The lean solvent inlet of poor rich liquid heat exchanger and the tower reactor liquid outlet of desorber connect, the lean solvent outlet of the poor rich liquid heat exchanger
It is connect with the inlet on absorption tower, so that the lean solvent of desorber is delivered to rich or poor liquid exchanger, flash tank from tower reactor liquid outlet
Outlet liquid be delivered to rich or poor liquid exchanger through the tank bottom liquid outlet of flash tank, lean solvent and rich solution in rich or poor liquid exchanger
Heat exchange is carried out, the temperature of lean solvent can not only be reduced, allows to pass back into absorption tower and is re-used as absorbent use, mention
High-selenium corn effect, and the temperature of the rich solution of input desorber can be improved, and then reduce the steam consumption of desorber, reduce energy
Consumption.
4. oil refinery dry gas recovery system provided by the utility model, the air inlet on the absorption tower be located at absorption tower from lower and
On 2-5 block column plate between on corresponding side wall, the inlet on the absorption tower is located at the top-down 1st piece of tower in absorption tower
On the corresponding side wall of plate, gas outlet is located at absorption tower tower top, and liquid outlet is located at absorbing tower bottom, so that gas is from tower bottom air inlet tower
Gas is ejected, liquid goes out liquid from tower bottom again from tower top feed liquor, can guarantee that gas phase and liquid phase come into full contact with, and reaches optimal mass transfer effect
Fruit.
Detailed description of the invention
It, below will be right in order to illustrate more clearly of specific embodiment of the present invention or technical solution in the prior art
Specific embodiment or attached drawing needed to be used in the description of the prior art are briefly described, it should be apparent that, it is described below
In attached drawing be that some embodiments of the utility model are not paying creativeness for those of ordinary skill in the art
Under the premise of labour, it is also possible to obtain other drawings based on these drawings.
Fig. 1 is the process flow chart of the oil refinery dry gas recovery system of the utility model.
Description of symbols:
1, residue gas compressor；2, it is dehydrated demercuration bed；3, ice chest；4, absorption tower；5, flash tank；6, desorber；7, rich or poor liquid
Heat exchanger；8, deoxidation adds hydrogen bed.
Specific embodiment
The technical solution of the utility model is clearly and completely described below in conjunction with attached drawing, it is clear that described
Embodiment is the utility model a part of the embodiment, instead of all the embodiments.Based on the embodiments of the present invention, originally
Field those of ordinary skill every other embodiment obtained without making creative work belongs to practical
Novel protected range.
In addition, as long as technical characteristic involved in the utility model different embodiments disclosed below is each other
Not constituting conflict can be combined with each other.
Embodiment 1
A kind of specific embodiment of oil refinery dry gas recovery system as shown in Figure 1, including the compression of sequentially connected dry gas
Machine, deoxidation add hydrogen bed, dehydration demercuration bed, ice chest, absorption tower, flash tank and desorber, the feed(raw material)inlet of the residue gas compressor
It being connect with the raw material conveying device for supplying oil refinery dry gas, the tower top gas outlet of the desorber connects product conveying device,
The first entrance of the product conveying device is connect with the tower top gas outlet of the desorber, and the second of the product conveying device
Entrance is connect with the ice chest.
The oil refinery dry gas of low pressure is transformed into the oil refinery dry gas of high temperature and pressure by doing work by the residue gas compressor, described de-
Oxygen adds hydrogen bed to use for removing the impurity such as alkynes, alkadienes, nitrogen oxides and oxygen in oil refinery dry gas, the dehydration demercuration bed
The impurity such as mercury, water in removing oil refinery dry gas.Wherein, the deoxidation adds the outlet of the air inlet connection residue gas compressor of hydrogen bed
Mouthful, the deoxidation adds the gas outlet of hydrogen bed to connect the entrance for being dehydrated demercuration bed.
The gas outlet of the ice chest and the air inlet on absorption tower connect, and are additionally provided on the ice chest for the first coolant flow
It passes to the first coolant entrance for recycling its cooling capacity and the first coolant outlet and is passed to for the second coolant flow and recycle its cooling capacity
The second coolant entrance and the second coolant outlet, the first coolant entrance of the ice chest and the tower top gas outlet on absorption tower
Connection, the second coolant entrance of the ice chest and the tank deck gas outlet of flash tank connect, and the second coolant of the ice chest goes out
Mouth is connect with the second entrance of product conveying device.
Oil refinery dry gas is successively delivered to ice chest after deoxidation dehydrogenation, dehydration demercuration removal of impurities, at the same time in absorption tower not
The fuel gas of three component of carbon containing two component or carbon is delivered to after exporting from the tower top gas outlet on absorption tower as the first coolant
Ice chest is delivered to ice chest as the second coolant after the output of tank deck gas outlet containing two component gas phase product of carbon in flash tank,
Oil refinery dry gas is exchanged with the tank deck gas of absorption tower overhead gas and flash tank progress heat simultaneously in ice chest, high temperature and pressure
Oil refinery dry gas is transformed into the oil refinery dry gas of cryogenic high pressure.
Wherein, the inlet of the flash tank and the tower reactor liquid outlet on absorption tower connect, the tank deck outlet of the flash tank
Mouth is connect with the second coolant entrance of ice chest, and the tank bottom liquid outlet of the flash tank and the inlet of desorber connect；Flash distillation
Tank is used to reduce rapidly the high pressure saturated solution i.e. pressure of high pressure rich solution exported from absorption tower tower reactor, rich due to the reduction of pressure
Some hydrocarbon gasification in liquid becomes gas and separates from liquid, is delivered to ice chest recycling cooling capacity through tank deck gas outlet,
Then it is exported by product conveying device.
It further include poor rich liquid heat exchanger in the present embodiment, unvaporized rich solution continues through poor rich liquid heat exchanger in flash tank
It is delivered to desorber, the tower reactor for stating poor rich liquid heat exchanger for rich solution and desorber that the tank bottom liquid outlet for flash tank exports goes out
The lean solvent of liquid mouth output carries out heat exchange, and the rich solution entrance of the poor rich liquid heat exchanger and the tank bottom of the flash tank go out liquid
The inlet of mouthful connection, the rich solution outlet of the poor rich liquid heat exchanger and desorber connects, the poor rich liquid heat exchanger it is poor molten
The connection of the tower reactor liquid outlet of agent entrance and desorber, the lean solvent outlet of the poor rich liquid heat exchanger and the inlet on absorption tower connect
It connects；The lean solvent of desorber is delivered to rich or poor liquid exchanger from tower reactor outlet, while the rich solution of flash tank is from the tank bottom of flash tank
Liquid outlet is delivered to rich or poor liquid exchanger, and lean solvent and rich solution carry out heat exchange, lean solvent temperature drop in rich or poor liquid exchanger
It is delivered to absorption tower after low to be recycled as absorbent, while being delivered to desorber after the raising of rich solution temperature, can not only drop
The temperature of low lean solvent allows to pass back into absorption tower and is re-used as absorbent use, improves assimilation effect, and can mention
The temperature of the rich solution of height input desorber, and then the steam consumption of desorber is reduced, reduce energy consumption.
For desorber for separating absorbed two component of carbon, three component of carbon with absorbent, the desorber is plate
Formula tower or packed tower, the desorption mode are steam desorption；Two component of carbon, three component of carbon after separation is in gaseous form from solution
The output of product conveying device is passed through in the tower top output for inhaling tower.
Wherein, the absorption tower can using plate column perhaps the packed tower desorber can using plate column or
Packed tower.
In the present embodiment, the absorption tower and desorber are plate column, and the theoretical cam curve on the absorption tower is 20-30
Block, the theoretical cam curve of the desorber are 3-20 block.
In order to guarantee that gas phase and liquid phase come into full contact with, mass transfer effect is improved, the air inlet on the absorption tower is located at absorption tower
The corresponding side-walls of 2-5 block column plate from bottom to top, the inlet on the absorption tower are located at top-down 1st piece of absorption tower
On the corresponding side wall of column plate.
The inlet of the desorber is located on the corresponding side wall of the top-down 1-4 block column plate of desorber.
The absorption tower tower reactor and desorption tower reactor are provided with reboiler.
Obviously, the above embodiments are merely examples for clarifying the description, and does not limit the embodiments.It is right
For those of ordinary skill in the art, can also make on the basis of the above description it is other it is various forms of variation or
It changes.There is no necessity and possibility to exhaust all the enbodiments.And it is extended from this it is obvious variation or
It changes among the protection scope created still in the utility model.
Claims (7)
1. a kind of oil refinery dry gas recovery system, which is characterized in that including sequentially connected residue gas compressor (1), dehydration demercuration bed
(2), ice chest (3), absorption tower (4), flash tank (5) and desorber (6)；
Wherein, the feed(raw material)inlet of the residue gas compressor (1) is connect with the raw material conveying device for supplying oil refinery dry gas, described
The tower top gas outlet of desorber (6) connects product conveying device, the first entrance of the product conveying device and the desorber
(6) tower top gas outlet connection, the second entrance of the product conveying device are connect with the ice chest (3)；
The gas outlet of the ice chest (3) is connect with the air inlet of absorption tower (4), is additionally provided on the ice chest (3) cold for first
But agent is circulated to recycle the first coolant entrance of its cooling capacity and the first coolant outlet and pass to recycling for the second coolant flow
The second coolant entrance and the second coolant outlet of its cooling capacity, the first coolant entrance and absorption tower (4) of the ice chest (3)
The connection of tower top gas outlet, the second coolant entrance of the ice chest (3) connect with flash tank (5), the second of the ice chest (3)
The connection of the second entrance of coolant outlet and product conveying device.
2. oil refinery dry gas recovery system according to claim 1, which is characterized in that the inlet of the flash tank (5) with
The tower reactor liquid outlet on absorption tower (4) connects, the tank deck gas outlet of the flash tank (5) and second coolant entrance of ice chest (3)
Connection, the tank bottom liquid outlet of the flash tank (5) are connect with the inlet of desorber (6).
3. oil refinery dry gas recovery system according to claim 2, which is characterized in that further include poor rich liquid heat exchanger (7), institute
Poor rich liquid heat exchanger (7) are stated for the rich solution of the tank bottom liquid outlet output for flash tank (5) and the tower reactor liquid outlet of desorber (6)
The lean solvent of output carries out heat exchange, and the rich solution entrance of the poor rich liquid heat exchanger (7) and the tank bottom of the flash tank (5) go out
The connection of liquid mouth, the rich solution outlet of the poor rich liquid heat exchanger (7) are connect with the inlet of desorber (6), the rich or poor liquid heat exchange
The lean solvent inlet of device (7) is connect with the tower reactor liquid outlet of desorber (6), the lean solvent outlet of the poor rich liquid heat exchanger (7)
It is connect with the inlet of absorption tower (4).
4. oil refinery dry gas recovery system according to any one of claim 1-3, which is characterized in that further include being connected to institute
The deoxidation stating residue gas compressor (1) and being dehydrated between demercuration bed (2) adds hydrogen bed (8), and the deoxidation adds the air inlet of hydrogen bed (8) to connect
The gas outlet of the residue gas compressor (1) is connect, the deoxidation adds the gas outlet of hydrogen bed (8) to connect the air inlet for being dehydrated demercuration bed (2)
Mouthful.
5. oil refinery dry gas recovery system according to any one of claim 1-3, which is characterized in that the absorption tower (4)
Theoretical cam curve be 20-30 block, the theoretical cam curve of the desorber (6) is 3-20 block.
6. oil refinery dry gas recovery system according to claim 5, which is characterized in that the air inlet position of the absorption tower (4)
In the corresponding side-walls of 2-5 block column plate of absorption tower (4) from bottom to top, the inlet of the absorption tower (4) is located at absorption tower
(4) the top-down 1st piece of corresponding side-walls of column plate.
7. oil refinery dry gas recovery system according to claim 5, which is characterized in that the inlet position of the desorber (6)
In positioned at the corresponding side-walls of desorber (6) top-down 1-4 block column plate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821397310.1U CN208959573U (en) | 2018-08-28 | 2018-08-28 | A kind of oil refinery dry gas recovery system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821397310.1U CN208959573U (en) | 2018-08-28 | 2018-08-28 | A kind of oil refinery dry gas recovery system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN208959573U true CN208959573U (en) | 2019-06-11 |
Family
ID=66753696
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201821397310.1U Active CN208959573U (en) | 2018-08-28 | 2018-08-28 | A kind of oil refinery dry gas recovery system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN208959573U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109045929A (en) * | 2018-08-28 | 2018-12-21 | 上海东化环境工程有限公司 | A kind of oil refinery dry gas recovery system and method |
| CN112410070A (en) * | 2020-10-15 | 2021-02-26 | 大连理工大学 | Energy-saving process and device for recovering carbon dioxide from refinery dry gas |
-
2018
- 2018-08-28 CN CN201821397310.1U patent/CN208959573U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109045929A (en) * | 2018-08-28 | 2018-12-21 | 上海东化环境工程有限公司 | A kind of oil refinery dry gas recovery system and method |
| CN112410070A (en) * | 2020-10-15 | 2021-02-26 | 大连理工大学 | Energy-saving process and device for recovering carbon dioxide from refinery dry gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109912379B (en) | Refinery dry gas separation method and device | |
| CN109678635B (en) | Saturated hydrocarbon cracking gas separation system and utilization method of ethane/propane-rich saturated hydrocarbon | |
| CN109045929A (en) | A kind of oil refinery dry gas recovery system and method | |
| CN100473715C (en) | Process flow for raw material pretreatment portion of catalytic dry gas produced phenylethane | |
| CN102382680B (en) | Combined technology of catalytic cracking absorbing stabilizing system and C3 intercooling oil absorption | |
| CN103588604B (en) | A kind of system and method combining carbon two in absorption process recovery oil refinery dry gas | |
| CN101759516B (en) | Method for refining catalysis drying gas by using oil absorption extraction | |
| CN104557387A (en) | Refinery mixed dry gas recovery system and recovery method | |
| CN107827698B (en) | Non-cryogenic separation method and system for ethylene-containing pyrolysis gas | |
| CN101759518A (en) | Method for absorbing and separating refinery catalytic dry gas by adopting oil | |
| CN104557384A (en) | Refinery mixed dry gas recovery system and recovery method | |
| CN208959573U (en) | A kind of oil refinery dry gas recovery system | |
| JP2022509733A (en) | Methods and systems for separating light hydrocarbons | |
| CN104557386B (en) | A kind of refinery's mixing dry gas recovery system and recovery method | |
| CN103030494B (en) | Absorption and hydration coupling device and method for separating ethylene and ethane in catalytic cracking dry gas or ethylene pyrolysis gas | |
| CN106609161B (en) | A kind of method of separating plant saturation dry gas | |
| CN107987885B (en) | Device and method for recovering carbon two and carbon three from catalytic dry gas | |
| CN104560194B (en) | Refinery saturated dry gas recovery system and recovery method | |
| CN111320523B (en) | Method and device for separating ethylene from refinery dry gas | |
| CN113354506B (en) | Method for recovering and separating low-carbon hydrocarbons from refinery saturated dry gas by combined absorption | |
| CN111004079A (en) | Separation method and device for preparing ethylene reaction gas through oxidative coupling of methane | |
| CN105647583A (en) | Novel absorption stabilizing technology and system | |
| CN109748771A (en) | The method for recycling carbon two in oil refinery dry gas | |
| CN112707787B (en) | Pyrolysis gas separation system with purification function and utilization method | |
| CN211871870U (en) | System for recovering carbon second fraction in refinery dry gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |