CN105885913A - Process for recovering light hydrocarbon in atmospheric and vacuum distillation unit - Google Patents
Process for recovering light hydrocarbon in atmospheric and vacuum distillation unit Download PDFInfo
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- CN105885913A CN105885913A CN201510016463.1A CN201510016463A CN105885913A CN 105885913 A CN105885913 A CN 105885913A CN 201510016463 A CN201510016463 A CN 201510016463A CN 105885913 A CN105885913 A CN 105885913A
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Abstract
The invention discloses a process for recovering light hydrocarbon in an atmospheric and vacuum distillation unit to overcome the defects that in the prior art, equipment occupies a large area, equipment maintenance workload is large, investment is high, and the process is complicated. According to a method, crude oil enters a primary tower after being heated, oil gas on the top of the primary tower enters primary top oil gas cold exchange equipment, material flow discharged out of the primary top oil gas cold exchange equipment enters a primary top product and backflow tank, a part of a liquid phase in the primary top product and backflow tank serves as backflow to be returned to the primary tower, the other part of the liquid phase is conveyed to a light hydrocarbon recovery unit, oil at the bottom of the primary tower enters the lower portion of an atmospheric tower after being heated, oil gas on the top of the atmospheric tower enters the light hydrocarbon recovery unit after first-level condensation or second-level condensation, and dry gas, liquefied gas, naphtha and the like are separated. Stable naphtha is injected in an oil gas pipeline on the top of the primary tower and an oil gas pipeline on the top of the atmospheric tower, or low-temperature condensing equipment is arranged and meanwhile stable naphtha is injected, so that all light hydrocarbon components in the oil gas are condensed in an oil phase.
Description
Technical field
The invention belongs to atmospheric and vacuum distillation field, particularly to light hydrocarbon component in a kind of fore-running-atmospheric distillation plant
Recovery process.
Background technology
The recovery of atmospheric and vacuum distillation unit light hydrocarbon component at present mainly has two schemes, and one is " compressor side
Case "；Another kind is " compressor-free scheme ", also referred to as " primary distillation tower pressure boosting operation scheme ".
" compressor scheme " has again two kinds of methods, and most common of which one is: atmospheric and vacuum distillation unit normal pressure part is adopted
With flash distillation-air-distillation process program, often top return tank separate containing light hydrocarbon oil-gas, boost (about through compressor
1.0MPa) mix with the often top oil after part boosting afterwards so that it is be dissolved in this part and often push up in oil, this part
Lighter hydrocarbons recovery unit delivered to respectively by often top oil after often top oil boosts with another part.Lighter hydrocarbons recovery unit can
Set as required four-column process flow (i.e. absorption, desorbing, stable, re-absorption), three-column process flow (i.e. absorption, desorbing,
Stable), double-column process (only stabilizer and absorption tower) or single column flow process (only stabilizer), reclaim it
In liquefied gas.
Another kind of " compressor scheme ", such as the Chinese patent of Application No. 00125975.X, this technology discloses
A kind of atmospheric and vacuum distillation unit reclaims the technique of lighter hydrocarbons, and its method is to use fore-running-air-distillation process program,
Just, often push up oil gas and deliver to absorption tower after compressor boosting, use the often oily absorption in top light hydrocarbon component therein, so
Together sending into stabilizer with just top oil afterwards, tower top goes out liquefied petroleum gas product, goes out to stablize Petroleum at the bottom of tower；With
Time, control to stablize the temperature and pressure of tower top so that it is discharge gas absorbs to absorption tower.
In compressor scheme, because compressor is dynamic equipment (need one open one standby) so that equipment take up an area many, set
Standby maintenance workload greatly, costly, investment is high, flow process is complicated, operator are many, energy consumption of compressor is high
Shortcoming.
Compressor-free reclaims lighter hydrocarbons scheme.Disclosed in as interim in " oil refining design " 1996 volume 26 the 2nd
Article, entitled " reclaiming the distilling apparatus design of lighter hydrocarbons without compressor ".The program uses fore-running-normal pressure to steam
Evaporate process program, primary distillation tower pressure boosting operation (operation pressure is typically at 0.2-0.5MPa), make in crude oil big
The light hydrocarbon component of amount is dissolved in first apex stone cerebrol, and remaining small part light hydrocarbon component is dissolved in Chang Dingshi cerebrol
In, just, Chang Dingshi cerebrol send after pump boosts lighter hydrocarbons recovery unit (lighter hydrocarbons recovery unit can set single column flow process,
Double-column process, three-column process flow and four-column process flow) carry out fractional distillation, the liquefied gas that output is qualified.
Program compressor-free, overall merit is many, and one comes out, and is widely adopted.But it is (interior to need to set primary distillation tower
If about more than 20 layer tower tray), and primary distillation tower wants pressure boosting operation, which increases equipment investment and energy consumption.
Summary of the invention
It is an object of the invention to provide a kind of new technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons.Existing to overcome
When having flash distillation-normal pressure technology to use compressor scheme, equipment take up an area many, plant maintenance workload greatly, costly,
The shortcomings such as investment height, flow process complexity and energy consumption of compressor are high.
The present invention provides the first technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons, it is characterised in that: crude oil warp
Entering primary distillation tower after intensification, the tower top oil gas of primary distillation tower enters just top oil gas cold exchange device, cold from just top oil gas
Exchange device logistics out enters just top product and return tank, just pushes up the liquid phase part one in product and return tank
Part returns primary distillation tower as backflow, and another part send lighter hydrocarbons recovery unit, and the tower base oil of primary distillation tower is through heating up
Rear entrance atmospheric tower bottom, the tower top oil gas of atmospheric tower enters often top oil gas cold exchange device, cold from often top oil gas
Exchange device logistics out enters often top product and return tank, often top product and the atmospheric overhead warp of return tank
After boosting, a part returns to atmospheric tower top as backflow, and remainder send lighter hydrocarbons recovery unit to separate dry gas
(C1、C2), liquefied gas (C3、C4) and Petroleum (C+ 5) etc., described at fore-running tower top to just pushing up product
Oil-gas pipeline between product and return tank and Atmospheric Tower are to often oil-gas pipeline between top product and return tank
Petroleum is stablized in upper injection, and the oil-gas pipeline between fore-running tower top to just top product reflux tank stablizes Petroleum
Injection rate is 0.5～100 weight % just pushing up oil and gas content, the oil between Atmospheric Tower to often top product reflux tank
The injection rate stablizing Petroleum on gas pipeline is 0.5～100 weight % often pushing up oil and gas content, stablizes Petroleum
Injection rate so that in oil gas light hydrocarbon component all coagulate in oil phase.
The first technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons is technically characterized in that further described just pushes up product
The temperature of product and return tank is 30～60 DEG C, and pressure is gauge pressure 0.005～0.1MPa.
The first technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons is technically characterized in that is produced from described normal top further
The temperature of product and return tank is 30～60 DEG C, and pressure is gauge pressure 0.005～0.1MPa.
The first technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons is technically characterized in that further described stablizes stone
The particular location that cerebrol injects, depending on the temperature and pressure stablizing Petroleum, stablizes Petroleum pressure and is more than
The pressure of decanting point tower top oil gas, it is ensured that stablizing Petroleum can inject smoothly；Stablize Petroleum temperature and injection
The temperature difference of the overhead oil temperature of point is the smaller the better, generally-100 DEG C～+100 DEG C.
The first technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons is technically characterized in that further described just pushes up oil
Air cooling exchange device and often top oil gas cold exchange device refer in heat exchanger, air cooler and recirculated water cooling condenser etc. at least
A kind of.
The present invention provides the technique that the second reclaims atmospheric and vacuum distillation unit lighter hydrocarbons, it is characterised in that: crude oil warp
Entering primary distillation tower after intensification, the tower top oil gas of primary distillation tower enters just top oil gas cold exchange device, cold from just top oil gas
Exchange device logistics out enters just top product and return tank, just pushes up the liquid phase part in product and return tank
Returning primary distillation tower as backflow, another part send lighter hydrocarbons recovery unit, and the tower base oil of primary distillation tower is laggard through heating up
Entering atmospheric tower bottom, the tower top oil gas of atmospheric tower uses condensed in two stages, the most often top primary oil air cooling exchange device,
Enter often top return tank after partial condensation to separate, after the oil phase that separates is boosted, be divided into two parts, one
Being allocated as returning to atmospheric tower top for backflow, another part often pushes up two together with the oil gas that often top return tank separates
Enter after level oil gas cold exchange device and often push up products pot, after often the oil phase of top products pot is boosted, send lighter hydrocarbons recovery list
Unit, separates dry gas, liquefied gas and Petroleum at lighter hydrocarbons recovery unit, and returns to just top product at fore-running tower top
Oil-gas pipeline and Atmospheric Tower between stream tank stablize stone to often pushing up injection on the oil-gas pipeline between products pot
Cerebrol, fore-running tower top to just pushing up the injection rate stablizing Petroleum on the oil-gas pipeline between product and return tank is
Just push up 0.5～100 weight % of oil and gas content, stable on the oil-gas pipeline between Atmospheric Tower to often top products pot
The injection rate of Petroleum is 0.5～100 weight % often pushing up oil and gas content, stablizes the injection rate of Petroleum so that oil
In gas, light hydrocarbon component all coagulates in oil phase.
The second reclaims the technique of atmospheric and vacuum distillation unit lighter hydrocarbons and is technically characterized in that further and described just pushes up product
The temperature of product and return tank is 30～60 DEG C, and pressure is gauge pressure 0.005～0.1MPa.
The second reclaims the technique of atmospheric and vacuum distillation unit lighter hydrocarbons and is technically characterized in that described normal fight back further
The temperature of stream tank is 35～120 DEG C, and pressure is gauge pressure 0.01～0.15MPa.
The second reclaims the technique of atmospheric and vacuum distillation unit lighter hydrocarbons and is technically characterized in that is produced from described normal top further
The temperature of product tank is 30～60 DEG C, and pressure is gauge pressure 0.005～0.1MPa.
The second reclaims the technique of atmospheric and vacuum distillation unit lighter hydrocarbons and is technically characterized in that further and described just pushes up oil
Air cooling exchange device, often top primary oil air cooling exchange device and often two grades of top oil gas cold exchange devices refer respectively to heat exchanger,
At least one in air cooler and recirculated water cooling condenser etc..
The second reclaims the technique of atmospheric and vacuum distillation unit lighter hydrocarbons and is technically characterized in that further and described stablizes stone
The particular location that cerebrol injects, depending on the temperature and pressure stablizing Petroleum, stablizes Petroleum pressure and is more than
The pressure of decanting point tower top oil gas, it is ensured that stablizing Petroleum can inject smoothly；Stablize Petroleum temperature and decanting point
The temperature difference of overhead oil temperature is the smaller the better, generally-100 DEG C～+100 DEG C；Wherein normal teeming access point position
Put the most often top return tank to push up between products pot to normal.
The present invention provides the third technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons, it is characterised in that: crude oil warp
Entering primary distillation tower after intensification, the tower top oil gas of primary distillation tower sequentially passes through and just pushes up oil gas cold exchange device and just push up oil gas
After condensation at low temperature equipment, temperature is 1～50 DEG C, and pressure is 0.005～0.1MPa, enters and just pushes up product and return
Stream tank, the liquid phase part just pushed up in product and return tank returns primary distillation tower as backflow, and another part send gently
Hydrocarbon recovery unit, the tower base oil of primary distillation tower enters atmospheric tower bottom, the tower top oil gas warp of atmospheric tower after heating up
After often pushing up oil gas cold exchange device and often top oil gas condensation at low temperature equipment cooling, temperature is 1～50 DEG C, and pressure is
0.005～0.1MPa, enter often top product and return tank, often the often top oil of top product and return tank is boosted
After, a part returns to atmospheric tower top as backflow, and remainder send lighter hydrocarbons recovery unit to separate dry air-liquid
Activating QI and Petroleum.At fore-running tower top to just pushing up the oil-gas pipeline between product and return tank and Atmospheric Tower
Stablizing Petroleum to often pushing up to inject on the oil-gas pipeline between product and return tank, fore-running tower top is to just pushing up product
And the injection rate stablizing Petroleum on the oil-gas pipeline between return tank is just to push up 0.1～100 weights of oil and gas content
Amount %, Atmospheric Tower is normal to often pushing up the injection rate stablizing Petroleum on the oil-gas pipeline between product and return tank
0.1～100 weight % of top oil and gas content, stablize the injection rate of Petroleum so that light hydrocarbon component all coagulates in oil gas
In oil phase.
The third technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons is technically characterized in that further described just pushes up oil
Gas condensation at low temperature equipment and often top coolant media used by oil gas low-temperature condenser are from the chilled water system of this device
Make unit or other device.
The third technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons is technically characterized in that further described just pushes up product
The temperature of product and return tank is 1～50 DEG C, and pressure is gauge pressure 0.005～0.1MPa.
The third technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons is technically characterized in that is produced from described normal top further
The temperature of product and return tank is 1～50 DEG C, and pressure is gauge pressure 0.005～0.1MPa.
The third technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons is technically characterized in that further described stablizes stone
The particular location that cerebrol injects, depending on the temperature and pressure stablizing Petroleum, stablizes Petroleum pressure and is more than
The pressure of decanting point tower top oil gas, it is ensured that stablizing Petroleum can inject smoothly；Stablize Petroleum temperature and decanting point
The temperature difference of overhead oil temperature the smaller the better, generally-100 DEG C～+100 DEG C.
The third technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons is technically characterized in that further described just pushes up oil
Air cooling exchange device and often top oil gas cold exchange device refer in heat exchanger, air cooler and recirculated water cooling condenser etc. respectively
At least one.
The technique that the present invention provides the 4th kind of recovery atmospheric and vacuum distillation unit lighter hydrocarbons, it is characterised in that: crude oil warp
Entering primary distillation tower after intensification, the tower top oil gas of primary distillation tower sequentially enters and just pushes up oil gas cold exchange device and just push up oil gas
After condensation at low temperature equipment, temperature is 1～50 DEG C, and pressure is 0.005～0.1MPa, enters and just pushes up product and return
Stream tank, just the liquid phase part in the product reflux tank of top returns primary distillation tower as backflow, and another part send lighter hydrocarbons
Recovery unit, the tower base oil of primary distillation tower enters atmospheric tower bottom after heating up, and the tower top oil gas of atmospheric tower is frequent
After the primary oil air cooling exchange device condensation of top, temperature is 35～120 DEG C, and pressure is 0.01～0.15MPa, enters
Entering often top return tank to separate, the oil phase separated is divided into two parts, and boosted rear portion is returned as backflow
Going back to atmospheric tower top, another part often pushes up two grades of cold changing of oil gas together with the oil gas that often top return tank separates and sets
After standby and often two grades of top oil gas condensation at low temperature equipment cooling, temperature is 1～50 DEG C, pressure be 0.005～
0.1MPa, enters and often pushes up products pot, and often the oil phase of top products pot send lighter hydrocarbons recovery unit, at lighter hydrocarbons recovery list
Unit separates dry gas, liquefied gas and Petroleum, at fore-running tower top to just pushing up the Oil/Gas Pipe between product and return tank
Line and Atmospheric Tower stablize Petroleum to often pushing up injection on the oil-gas pipeline between products pot, and fore-running tower top is extremely
The injection rate just stablizing Petroleum on the oil-gas pipeline between top product and return tank is just to push up oil and gas content
0.1～100 weight %, the oil-gas pipeline between Atmospheric Tower to often top products pot is stablized the injection of Petroleum
Amount, for often pushing up 0.1～100 weight % of oil and gas content, stablizes the injection rate of Petroleum so that light hydrocarbon component in oil gas
All coagulate in oil phase.
The technique of the 4th kind of recovery atmospheric and vacuum distillation unit lighter hydrocarbons is technically characterized in that further described just pushes up oil
Gas condensation at low temperature equipment and often top coolant media used by two grades of oil gas condensation at low temperature equipment are chilled water, from this
The chilled water of device or other device.
The technique of the 4th kind of recovery atmospheric and vacuum distillation unit lighter hydrocarbons is technically characterized in that further described just pushes up product
The temperature of product and return tank is 1～50 DEG C, and pressure is gauge pressure 0.005～0.1MPa.
The technique of the 4th kind of recovery atmospheric and vacuum distillation unit lighter hydrocarbons is technically characterized in that described normal fight back further
The temperature of stream tank is 35～120 DEG C, and pressure is gauge pressure 0.01～0.15MPa.
The technique of the 4th kind of recovery atmospheric and vacuum distillation unit lighter hydrocarbons is technically characterized in that is produced from described normal top further
The temperature of product tank is 1～50 DEG C, and pressure is gauge pressure 0.005～0.1MPa.
The technique of the 4th kind of recovery atmospheric and vacuum distillation unit lighter hydrocarbons is technically characterized in that further described just pushes up oil
Air cooling exchange device, often top primary oil air cooling exchange device and often two grades of top oil gas cold exchange devices refer respectively to heat exchanger,
At least one in air cooler and recirculated water cooling condenser etc..
The technique of the 4th kind of recovery atmospheric and vacuum distillation unit lighter hydrocarbons is technically characterized in that further described stablizes stone
The particular location that cerebrol injects, depending on the temperature and pressure stablizing Petroleum, stablizes Petroleum pressure and is more than
The pressure of decanting point tower top oil gas, it is ensured that stablizing Petroleum can inject smoothly；Stablize Petroleum temperature and injection
The temperature difference of some overhead oil temperature is the smaller the better, generally-100 DEG C～+100 DEG C.Wherein normal teeming access point
Return tank is the most often pushed up to often pushing up between products pot in position.
Petroleum of stablizing of the present invention is from this device or other device.
The technique of recovery atmospheric and vacuum distillation unit lighter hydrocarbons of the present invention can be used in atmospheric and vacuum distillation unit light
The recovery of hydrocarbon component.The technology of the present invention compared with prior art has the advantage that as follows:
1) fore-running-atmospheric processes of the present invention, can ensure under conditions of atmospheric and vacuum distillation unit routine operation,
Stablize Petroleum by adding in tower top In Oil-gas Line, or use overhead system inject stablize Petroleum with
The method that condensation at low temperature combines, improves the absorbability of Petroleum, makes just, often pushes up light hydrocarbon component in oil gas
Can be the most molten in over-head naphtha, thus boost through pump, it is sent to lighter hydrocarbons recovery unit, reclaims its liquid
Activating QI.This method is simple and practical.
2) atmospheric and vacuum distillation unit reclaims two schemes (" compressor scheme " and " primary distillation tower that lighter hydrocarbons are main at present
Pressure boosting operation scheme ") in, " primary distillation tower pressure boosting operation scheme " energy consumption is higher (higher about than the present invention program
0.2kgoe/t crude oil), " compressor scheme " one-time investment equipment maintenance cost high, dynamic is high, it is many to take up an area,
The shortcomings such as operator are many, process Processing High-sulfur High-Acidity Crude Oils especially, higher to material, the performance requirement of compressor,
Investment is bigger, and equipment maintenance cost is higher, and compressor electricity consumption is many, and energy consumption is high (higher about than the present invention program
0.04-0.07kgoe/t crude oil).Use the inventive method, inject in overhead system and stablize Petroleum, or
It is to inject in overhead system to stablize Petroleum and method that condensation at low temperature combines, tower top gas and oil equilibration can be changed
State, makes tower top oil gas all be dissolved in Petroleum.Stablize Petroleum from this device lighter hydrocarbons recovery unit
At the bottom of stabilizer, it is possible to quoted from outer device.Although stablizing Petroleum in overhead system injection can increase lighter hydrocarbons recovery
Unit stabilizer reboiler load, but total energy consumption is the most relatively low.
By the drawings and specific embodiments, the present invention is described in further detail below, but is not limiting as this
Bright scope.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of the first recovery atmospheric and vacuum distillation unit lighter hydrocarbons of the present invention.
Fig. 2 is the process flow diagram that the second of the present invention reclaims atmospheric and vacuum distillation unit lighter hydrocarbons.
Fig. 3 is the process flow diagram of the third recovery atmospheric and vacuum distillation unit lighter hydrocarbons of the present invention.
Fig. 4 is the process flow diagram of the 4th kind of recovery atmospheric and vacuum distillation unit lighter hydrocarbons of the present invention.
Reference shown in figure is:
1-primary distillation tower, 2-atmospheric pressure kiln, 3-atmospheric tower, 4-often pushes up oil gas cold exchange device, and 5-often pushes up oil gas low temperature cold
Solidifying equipment, 6-often pushes up product and return tank, and 7-often pushes up product and backflow oil pump, and 8-often pushes up primary oil air cooling and changes and set
Standby, 9-often pushes up return tank, 10-normal fight back stream oil pump, and 11-often pushes up two grades of oil gas cold exchange devices, and 12-often pushes up two
Level oil gas condensation at low temperature equipment, 13-often pushes up products pot, and 14-often pushes up product oil pump, 15-feed surge tank, 16-
Absorption tower, 17-desorber, 18-stabilizer, 19-stablizes return tank of top of the tower, and 20-stablizes Petroleum cooler,
Push up at the beginning of 21-to push up at the beginning of oil gas cold exchange device, 22-and at the beginning of oil gas condensation at low temperature equipment, 23-, push up product and return tank, 24-
Just top product and backflow oil pump.
Detailed description of the invention
As it is shown in figure 1, Fig. 1 is the first technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons.Crude oil is through heating up
Rear entrance primary distillation tower 1, the tower top oil gas of primary distillation tower 1 enters just top oil gas cold exchange device 21, pushes up oil gas from just
Cold exchange device 21 logistics out enters just top product and return tank 23, and the tower top at primary distillation tower 1 pushes up to first
Injecting on oil-gas pipeline between oil gas cold exchange device 21 and stablize Petroleum, injection rate is the tower top of primary distillation tower 1
(stablizing Petroleum can also be at just top oil gas cold exchange device 21 to just pushing up product for 0.5-100 weight % of oil and gas content
Inject on oil-gas pipeline between product return tank 23, be only one of which situation shown in Fig. 1) so that all
Gas is dissolved in Petroleum, and under normal circumstances, just top product and return tank 23 are without gas emissions, just push up
A liquid phase part in product and return tank 23 returns primary distillation tower 1 as backflow, and another part send lighter hydrocarbons recovery
Feed surge tank 15 in unit, the tower base oil of primary distillation tower 1 enters atmospheric tower 3 after atmospheric pressure kiln 2 heats up
Bottom, the tower top oil gas of atmospheric tower 3 enters often top oil gas cold exchange device 4, from often top oil gas cold exchange device 4
Logistics out enters often top product and return tank 6, and the tower top at atmospheric tower 3 pushes up oil gas cold exchange device 4 to normal
Between oil-gas pipeline on inject stablize Petroleum, injection rate is the 0.5-100 of the overhead oil tolerance of atmospheric tower 3
(stablizing Petroleum can also be at often top oil gas cold exchange device 4 to often between top product and return tank 6 for weight %
Oil-gas pipeline on inject, be only one of which situation shown in Fig. 1) so that all gas is dissolved in stone
In cerebrol, under normal circumstances, often the gas outlet of top product and return tank 6 is without gas emissions, often pushes up product
After the atmospheric overhead of product and return tank 6 often pushes up product and backflow oil pump 7 boosting, a part is as backflow
Return atmospheric tower 3 top, remainder send lighter hydrocarbons recovery feed surge tank 15, after through absorption tower 16,
Desorber 17, stabilizer 18 and stablize return tank of top of the tower 19, separate dry gas (C1、C2), liquefied gas (C3、
C4) and Petroleum (C+ 5), at the tower top of atmospheric tower 3 to the Oil/Gas Pipe between often top oil gas cold exchange device 4
The stable Petroleum injected on line is from the bottom of stabilizer 18 tower.
In the technique of the first recovery atmospheric and vacuum distillation unit lighter hydrocarbons described, just top product and the temperature of return tank 23
Degree is for 30-60 DEG C, and pressure is gauge pressure 0.005-0.1MPa, and just the lighter hydrocarbons in the oil gas of top are all dissolved in stone brain
In oil.
In the technique of the first recovery atmospheric and vacuum distillation unit lighter hydrocarbons described, often top product and the temperature of return tank 6
Degree is for 30-60 DEG C, and pressure is gauge pressure 0.005-0.1MPa, and the lighter hydrocarbons in Atmospheric Tower oil gas are all dissolved in
In Petroleum.
In the technique of the first recovery atmospheric and vacuum distillation unit lighter hydrocarbons described, the stable stone brain at the bottom of stabilizer 18 tower
Oil, a portion is injected into after stablizing Petroleum cooler 20 cooling and just pushes up and in overhead system of atmospheric tower, Fig. 1
Shown in be that the tower top of primary distillation tower 1 is to the oil-gas pipeline between just top oil gas cold exchange device 21 and atmospheric tower 3
Tower top on the oil-gas pipeline between often top oil gas cold exchange device 4.
As in figure 2 it is shown, Fig. 2 is the technique that the second reclaims atmospheric and vacuum distillation unit lighter hydrocarbons.It is with Fig. 1's
Difference is: the tower top oil gas of atmospheric tower 3 enters often top primary oil air cooling exchange device 8, enters after heat exchange cooling
Often top return tank 9 separates, and is divided into two parts after liquid phase that often top return tank 9 separates is boosted, one
Being allocated as returning the top of atmospheric tower 3 for backflow, another part is warp together with the oil gas that often top return tank 9 separates
Often enter often top products pot 13, under normal circumstances, often top products pot 13 after the two grades of oil gas cold exchange devices 11 in top
Gas outlet without gas emissions, often the oil phase of top products pot 13 send after often pushing up product oil pump 14 boosting
Lighter hydrocarbons recovery unit, on the oil-gas pipeline between often top return tank 9 to the often two grades of oil gas cold exchange devices 11 in top
Inject and stablize Petroleum (being only the one of which situation of stable Petroleum injection phase shown in Fig. 2), injection rate
0.5-100 weight % for the overhead oil tolerance of atmospheric tower 3.
Described the second reclaims in the technique of atmospheric and vacuum distillation unit lighter hydrocarbons, just top product and the temperature of return tank 23
Degree is for 30-60 DEG C, and pressure is gauge pressure 0.005-0.1MPa, and just the lighter hydrocarbons in the oil gas of top are all dissolved in stone brain
In oil.
Described the second reclaims in the technique of atmospheric and vacuum distillation unit lighter hydrocarbons, and often the temperature of top return tank 9 is
35-120 DEG C, pressure is gauge pressure 0.01-0.15MPa.
Described the second reclaims in the technique of atmospheric and vacuum distillation unit lighter hydrocarbons, and often the temperature of top products pot 13 is
30-60 DEG C, pressure is gauge pressure 0.005-0.1MPa.
Stable Petroleum at the bottom of stabilizer 18 tower, a portion is after stablizing Petroleum cooler 20 cooling
It is injected into and often pushes up return tank 9 to often pushing up on the oil-gas pipeline between two grades of oil gas cold exchange devices 11.
As it is shown on figure 3, Fig. 3 is the third technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons.Crude oil is through heating up
Rear entrance primary distillation tower 1, the tower top oil gas of primary distillation tower 1 pushes up oil gas cold exchange device 21 through first and just push up oil gas successively
Condensation at low temperature equipment 22, enters just top product and return tank 23, just pushes up the liquid phase in product and return tank 23
A part returns primary distillation tower 1 as backflow, and another part send the feed surge tank 15 in lighter hydrocarbons recovery unit,
The tower base oil of primary distillation tower 1 enters the bottom of atmospheric tower 3, the overhead oil of atmospheric tower 3 after atmospheric pressure kiln 2 heats up
Gas the most often pushes up oil gas cold exchange device 4, often top oil gas condensation at low temperature equipment 5 and enters often top product and return tank
6, at just top oil gas cold exchange device 21 with just between the oil gas condensation at low temperature equipment 22 of top and often oil gas is cold on top changes
Equipment 4 stablizes Petroleum (institute in Fig. 3 to injecting on the oil-gas pipeline between often top oil gas condensation at low temperature equipment 5
Show it is only the one of which situation of stable Petroleum injection phase), injection rate is respectively primary distillation tower 1 and atmospheric tower
0.1-100 weight % of the overhead oil tolerance of 3, so that all gas is dissolved in Petroleum, under normal circumstances,
Just the gas outlet of top product and return tank 23 and normal top product and return tank 6 is without gas emissions, often pushes up
After the atmospheric overhead of product and return tank 6 often pushes up product and backflow oil pump 7 boosting, a part is as returning
Stream return atmospheric tower 3 top, remainder enter feed surge tank 15, after through absorption tower 16, desorbing
Tower 17, stabilizer 18 and stablize return tank of top of the tower 19, separate dry gas (C1、C2), liquefied gas (C3、
C4) and Petroleum (C+ 5)。
In the technique of the third recovery atmospheric and vacuum distillation unit lighter hydrocarbons described, just top product and the temperature of return tank 23
Degree is for 1-50 DEG C, and pressure is gauge pressure 0.005-0.1MPa, and just the lighter hydrocarbons in the oil gas of top are all dissolved in Petroleum
In.
In the technique of the third recovery atmospheric and vacuum distillation unit lighter hydrocarbons described, often top product and the temperature of return tank 6
Degree is for 1-50 DEG C, and pressure is gauge pressure 0.005-0.1MPa, and the lighter hydrocarbons in Atmospheric Tower oil gas are all dissolved in stone
In cerebrol.
In the technique of the third recovery atmospheric and vacuum distillation unit lighter hydrocarbons described, the stable stone brain at the bottom of stabilizer 18 tower
Oil, a portion is injected into just top oil gas cold exchange device 21 He after stablizing Petroleum cooler 20 cooling
Just push up the oil-gas pipeline between oil gas condensation at low temperature equipment 22 and often push up oil gas cold exchange device 4 to often pushing up oil gas
On oil-gas pipeline between condensation at low temperature equipment 5.
Just top condensation at low temperature equipment 22 and often top cold media used by oil gas condensation at low temperature equipment 5 described in Fig. 3
Matter is chilled water, from system share engineering.
As shown in Figure 4, Fig. 4 is the technique of the 4th kind of recovery atmospheric and vacuum distillation unit lighter hydrocarbons.It is with Fig. 3's
Difference is: the tower top oil gas of atmospheric tower 3 enters often top primary oil air cooling exchange device 8, enters after heat exchange cooling
Often top return tank 9 separates, and is divided into two parts after liquid phase that often top return tank 9 separates is boosted, one
Being allocated as returning the top of atmospheric tower 3 for backflow, another part is warp together with the oil gas that often top return tank 9 separates
Often enter after two grades of oil gas condensation at low temperature equipment 12 of two grades of top oil gas cold exchange device 11 and normal top and often push up products pot
13, under normal circumstances, often the gas outlet of top products pot 13 is without gas emissions, often pushes up products pot 13
Oil phase send lighter hydrocarbons recovery unit after often pushing up product oil pump 14 boosting, at the often two grades of oil gas cold exchange devices 11 in top
Inject on oil-gas pipeline between the often two grades of oil gas condensation at low temperature equipment 12 in top and stablize Petroleum (institute in Fig. 4
Show it is only the one of which situation of stable Petroleum injection phase), injection rate is the overhead oil tolerance of atmospheric tower 3
0.1-100 weight %.
In the technique of described 4th kind of recovery atmospheric and vacuum distillation unit lighter hydrocarbons, just top product and the temperature of return tank 23
Degree is for 1-50 DEG C, and pressure is gauge pressure 0.005-0.1MPa, and just the lighter hydrocarbons in the oil gas of top are all dissolved in Petroleum
In.
In the technique of described 4th kind of recovery atmospheric and vacuum distillation unit lighter hydrocarbons, often the temperature of top return tank 9 is
35-120 DEG C, pressure is gauge pressure 0.01-0.15MPa.
In the technique of described 4th kind of recovery atmospheric and vacuum distillation unit lighter hydrocarbons, often the temperature of top products pot 13 is
1-50 DEG C, pressure is gauge pressure 0.005-0.1MPa.
Stable stone brain in the technique of described 4th kind of recovery atmospheric and vacuum distillation unit lighter hydrocarbons, at the bottom of stabilizer 18 tower
Oil, a portion is injected into just top oil gas cold exchange device 21 He after stablizing Petroleum cooler 20 cooling
Just the two grades of oil gas cold exchange devices 11 of oil-gas pipeline and normal top between the oil gas condensation at low temperature equipment 22 of top are to often
Push up on the oil-gas pipeline between two grades of oil gas condensation at low temperature equipment 12.
Described in Fig. 4, just top condensation at low temperature equipment 22 pushes up used by two grades of oil gas condensation at low temperature equipment 12 with normal
Coolant media is chilled water, from system share engineering.
Claims (24)
1. the technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons, it is characterised in that: crude oil enters after heating up
Primary distillation tower, the tower top oil gas of primary distillation tower enters just top oil gas cold exchange device, from just top oil gas cold exchange device out
Logistics enter just top product and return tank, just the liquid phase part part in top product and return tank is as returning
Stream returns primary distillation tower, and another part send lighter hydrocarbons recovery unit, and the tower base oil of primary distillation tower enters normal pressure after heating up
Tower bottom, the tower top oil gas of atmospheric tower enters often top oil gas cold exchange device, from often top oil gas cold exchange device out
Logistics enter often top product and return tank, after often the atmospheric overhead of top product and return tank is boosted, one
Part as backflow return atmospheric tower top, remainder send lighter hydrocarbons recovery unit separate dry gas, liquefied gas and
Petroleum, described in fore-running tower top to just oil-gas pipeline between top product and return tank and Atmospheric Tower extremely
Often inject on the oil-gas pipeline between top product and return tank and stablize Petroleum, fore-running tower top to just push up product and
Stablizing naphtha injection amount on oil-gas pipeline between return tank is 0.5～100 weight % just pushing up oil and gas content,
Atmospheric Tower is to often pushing up the injection rate stablizing Petroleum on the oil-gas pipeline between product and return tank for often pushing up oil
0.5～100 weight % of tolerance, stablize the injection rate of Petroleum so that light hydrocarbon component all coagulates at oil in oil gas
Xiang Zhong.
A kind of technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons the most according to claim 1, its feature exists
In: the temperature of described just top product and return tank is 30～60 DEG C, and pressure is gauge pressure 0.005～0.1MPa.
A kind of technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons the most according to claim 1, its feature exists
In: the temperature of described normal top product and return tank is 30～60 DEG C, and pressure is gauge pressure 0.005～0.1MPa.
A kind of technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons the most according to claim 1, its feature exists
In: the described particular location stablizing Petroleum injection, depending on the temperature and pressure stablizing Petroleum, stable
Petroleum pressure is more than the pressure of decanting point tower top oil gas, it is ensured that stablizes Petroleum and injects；Stablize Petroleum temperature
Degree is-100 DEG C～+100 DEG C with the temperature difference of the overhead oil temperature of decanting point.
A kind of technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons the most according to claim 1, its feature exists
In: described just top oil gas cold exchange device and often top oil gas cold exchange device refer to heat exchanger, air cooler and recirculated water cooling
At least one in condenser.
6. the technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons, it is characterised in that: crude oil enters after heating up
Primary distillation tower, the tower top oil gas of primary distillation tower enters just top oil gas cold exchange device, from just top oil gas cold exchange device out
Logistics enter just top product and return tank, just the liquid phase part in top product and return tank is returned as backflow
Returning primary distillation tower, another part send lighter hydrocarbons recovery unit, and the tower base oil of primary distillation tower enters under atmospheric tower after heating up
Portion, the tower top oil gas of atmospheric tower uses condensed in two stages, the most often top primary oil air cooling exchange device, partial condensation
Rear entrance is often pushed up return tank and is separated, and is divided into two parts after the oil phase that separates is boosted, and a part is as returning
Stream returns to atmospheric tower top, and it is cold that another part often pushes up two grades of oil gas together with the oil gas that often top return tank separates
Enter after exchange device and often push up products pot, after often the oil phase of top products pot is boosted, send lighter hydrocarbons recovery unit, gently
Hydrocarbon recovery unit separates dry gas, liquefied gas and Petroleum, at fore-running tower top to just between top product and return tank
Oil-gas pipeline and Atmospheric Tower stablize Petroleum, just to injecting on the oil-gas pipeline between often top products pot
Evaporate tower top to just pushing up the injection rate stablizing Petroleum on the oil-gas pipeline between product and return tank for just pushing up oil gas
0.5～100 weight % of amount, the oil-gas pipeline between Atmospheric Tower to often top products pot stablizes Petroleum
Injection rate is 0.5～100 weight % often pushing up oil and gas content, stablizes the injection rate of Petroleum so that lighter hydrocarbons in oil gas
Component is all coagulated in oil phase.
A kind of technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons the most according to claim 6, its feature exists
In: the temperature of described just top product and return tank is 30～60 DEG C, and pressure is gauge pressure 0.005～0.1MPa.
A kind of technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons the most according to claim 6, its feature exists
In: the temperature of described normal top return tank is 35～120 DEG C, and pressure is gauge pressure 0.01～0.15MPa.
A kind of technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons the most according to claim 6, its feature exists
In: the temperature of described normal top products pot is 30～60 DEG C, and pressure is gauge pressure 0.005～0.1MPa.
A kind of technique reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons the most according to claim 6, its feature
It is: described just top oil gas cold exchange device, often top primary oil air cooling exchange device and often two grades of cold the changing of oil gas in top set
For referring respectively at least one in heat exchanger, air cooler and recirculated water cooling condenser.
11. a kind of techniques reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons according to claim 6, its feature
It is: the described particular location stablizing Petroleum injection, depending on the temperature and pressure stablizing Petroleum, surely
Determine the Petroleum pressure pressure more than decanting point tower top oil gas, it is ensured that stablize Petroleum and inject；Stablize Petroleum temperature
Degree is-100 DEG C～+100 DEG C with the temperature difference of decanting point overhead oil temperature.
12. 1 kinds of techniques reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons, it is characterised in that: crude oil is laggard through heating up
Entering primary distillation tower, the tower top oil gas of primary distillation tower sequentially passes through just top oil gas cold exchange device and just top oil gas condensation at low temperature
After equipment, temperature is 1～50 DEG C, and pressure is 0.005～0.1MPa, enters just top product and return tank, just
A liquid phase part in top product and return tank returns primary distillation tower as backflow, and another part send lighter hydrocarbons recovery list
Unit, the tower base oil of primary distillation tower enters atmospheric tower bottom after heating up, and the tower top oil gas of atmospheric tower often pushes up oil gas
After cold exchange device and often top oil gas condensation at low temperature equipment, temperature is 1～50 DEG C, and pressure is 0.005～0.1MPa,
Entering often top product and return tank, after often the often top oil of top product and return tank is boosted, a part is as returning
Stream returns to atmospheric tower top, and remainder send lighter hydrocarbons recovery unit to separate dry gas, liquefied gas and Petroleum,
Fore-running tower top is to just pushing up the oil-gas pipeline between product and return tank and Atmospheric Tower to often top product and backflow
Inject on oil-gas pipeline between tank and stablize Petroleum, the oil gas between fore-running tower top to just top product reflux tank
The injection rate stablizing Petroleum on pipeline is 0.1～100 weight % just pushing up oil and gas content, and Atmospheric Tower is to often top
The injection rate stablizing Petroleum on oil-gas pipeline between product and return tank is often push up oil and gas content 0.1～100
Weight %, stablizes the injection rate of Petroleum so that light hydrocarbon component all coagulates in oil phase in oil gas.
13. a kind of techniques reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons according to claim 12, its feature
It is: described just top oil gas condensation at low temperature equipment and often top coolant media used by oil gas condensation at low temperature equipment are
Chilled water, from chilled water production unit or other device of this device.
14. a kind of techniques reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons according to claim 12, its feature
It is: the temperature of described just top product and return tank is 1～50 DEG C, and pressure is gauge pressure 0.005～0.1MPa.
15. a kind of techniques reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons according to claim 12, its feature
Being: the temperature of described normal top product and return tank is 1～50 DEG C, pressure is gauge pressure 0.005～0.1MPa.
16. a kind of techniques reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons according to claim 12, its feature
It is: the described particular location stablizing Petroleum injection, depending on the temperature and pressure stablizing Petroleum, surely
Determine the Petroleum pressure pressure more than decanting point tower top oil gas, it is ensured that stablize Petroleum and inject；Stablize Petroleum temperature
Degree is-100 DEG C～+100 DEG C with the temperature difference of the overhead oil temperature of decanting point.
17. a kind of techniques reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons according to claim 12, its feature
It is: described just top oil gas cold exchange device and often top oil gas cold exchange device refer to heat exchanger, air cooler and recirculated water
At least one in condenser.
18. 1 kinds of techniques reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons, it is characterised in that: crude oil is laggard through heating up
Entering primary distillation tower, the tower top oil gas of primary distillation tower sequentially enters just top oil gas cold exchange device and just top oil gas condensation at low temperature
After equipment, temperature is 1～50 DEG C, and pressure is 0.005～0.1MPa, enters just top product and return tank, just
A liquid phase part in top product and return tank returns primary distillation tower as backflow, and another part send lighter hydrocarbons recovery list
Unit, the tower base oil of primary distillation tower enters atmospheric tower bottom after heating up, and the tower top oil gas of atmospheric tower often pushes up one-level
After the cooling of oil gas cold exchange device, temperature is 35～120 DEG C, and pressure is 0.01～0.15MPa, enters often top
Return tank separates, and the oil phase separated is divided into two parts, and boosted rear portion returns normal pressure as backflow
Tower top, another part frequent two grades of oil gas cold exchange devices in top and normal together with the oil gas that often top return tank separates
After pushing up two grades of oil gas condensation at low temperature equipment coolings, temperature is 1～50 DEG C, and pressure is 0.005～0.1MPa,
Entering and often push up products pot, often the oil phase of top products pot send lighter hydrocarbons recovery unit, separates dry at lighter hydrocarbons recovery unit
Air-liquid activating QI and Petroleum, at fore-running tower top to just oil-gas pipeline between top product and return tank and often
Pressure tower top stablizes Petroleum to often pushing up injection on the oil-gas pipeline between products pot, and fore-running tower top is to just pushing up product
And the injection rate stablizing Petroleum on the oil-gas pipeline between return tank is just to push up 0.1～100 weights of oil and gas content
Amount %, the oil-gas pipeline between Atmospheric Tower to often top products pot is stablized the injection rate of Petroleum for often pushing up oil gas
0.1～100 weight % of amount, stablize the injection rate of Petroleum so that light hydrocarbon component all coagulates at oil phase in oil gas
In.
19. a kind of techniques reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons according to claim 18, its feature
It is: described just top oil gas condensation at low temperature equipment and often top cold media used by two grades of oil gas condensation at low temperature equipment
Matter is chilled water, from chilled water production unit or other device of this device.
20. a kind of techniques reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons according to claim 18, its feature
It is: the temperature of described just top product and return tank is 1～50 DEG C, and pressure is gauge pressure 0.005～0.1MPa.
21. a kind of techniques reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons according to claim 18, its feature
Being: the temperature of described normal top return tank is 35～120 DEG C, pressure is gauge pressure 0.01～0.15MPa.
22. a kind of techniques reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons according to claim 18, its feature
Being: the temperature of described normal top products pot is 1～50 DEG C, pressure is gauge pressure 0.005～0.1MPa.
23. a kind of techniques reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons according to claim 18, its feature
It is: described just top oil gas cold exchange device, often top primary oil air cooling exchange device and often two grades of cold the changing of oil gas in top set
For referring at least one in heat exchanger, air cooler and recirculated water cooling condenser.
24. a kind of techniques reclaiming atmospheric and vacuum distillation unit lighter hydrocarbons according to claim 18, its feature
It is: the described particular location stablizing Petroleum injection, depending on the temperature and pressure stablizing Petroleum, surely
Determine the Petroleum pressure pressure more than decanting point tower top oil gas, it is ensured that stablize Petroleum and inject；Stablize Petroleum
Temperature is-100 DEG C～+100 DEG C with the temperature difference of decanting point overhead oil temperature.
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| Application Number | Priority Date | Filing Date | Title |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107057747A (en) * | 2016-11-07 | 2017-08-18 | 中国石油大学(华东) | It is a kind of based on the energy-efficient deep drawing technique of Atmospheric vacuum clearly cut |
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| CN1454965A (en) * | 2003-05-08 | 2003-11-12 | 中国石化集团洛阳石油化工工程公司 | Petroleum atmospheric vacuum distillation process and unit |
| US20140353138A1 (en) * | 2012-01-17 | 2014-12-04 | Amit Sureshrao Amale | Process for vacuum distillation of a crude hydrocarbon stream |
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| CN1454965A (en) * | 2003-05-08 | 2003-11-12 | 中国石化集团洛阳石油化工工程公司 | Petroleum atmospheric vacuum distillation process and unit |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107057747A (en) * | 2016-11-07 | 2017-08-18 | 中国石油大学(华东) | It is a kind of based on the energy-efficient deep drawing technique of Atmospheric vacuum clearly cut |
| CN107057747B (en) * | 2016-11-07 | 2020-04-28 | 中国石油大学(华东) | Atmospheric-vacuum energy-saving deep drawing process based on clear cutting |
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