CN105885936A - Method for recycling light hydrocarbon with atmospheric and vacuum distillation device - Google Patents
Method for recycling light hydrocarbon with atmospheric and vacuum distillation device Download PDFInfo
- Publication number
- CN105885936A CN105885936A CN201510016671.1A CN201510016671A CN105885936A CN 105885936 A CN105885936 A CN 105885936A CN 201510016671 A CN201510016671 A CN 201510016671A CN 105885936 A CN105885936 A CN 105885936A
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- atmospheric
- oil
- tower
- oil gas
- lighter hydrocarbons
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Abstract
The invention discloses a method for recycling light hydrocarbon with an atmospheric and vacuum distillation device. The method aims at overcoming the defects that in the prior art, equipment is large in occupied area and maintenance workload, the investment is high, and the process is complex. The method includes the steps that crude oil enters a flash tower after being heated, oil gas at the top of the flash tower enters the middle upper portion of an atmospheric tower, oil at the bottom of the flash tower enters the lower portion of the atmospheric tower after being heated, oil gas at the top of the atmospheric tower enters a light hydrocarbon recycling unit after being subjected to first-stage condensation or second-stage condensation, and dry gas, liquefied gas, naphtha and the like are separated out, wherein low-temperature condensation equipment is arranged on an oil gas pipeline at the top of the atmospheric tower so that light hydrocarbon components in oil gas can be completely 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 flash distillation-atmospheric distillation plant
Recovery method.
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 portion
Point use flash distillation-air-distillation process program, often top return tank separate containing light hydrocarbon oil-gas, boost through compressor
(about 1.0MPa) mixes with the often top oil after part boosting afterwards so that it is is dissolved in this part and often pushes up in oil, this
Part is often pushed up the oil that often pushes up after oil boosts with another part and is delivered to lighter hydrocarbons recovery unit respectively.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. absorb,
Desorbing, stable), double-column process (only stabilizer and absorption tower) or single column flow process (only stabilizer),
Reclaim liquefied gas therein.
Another kind of " compressor scheme ", such as the Chinese patent of Application No. 00125975.X, this technology is open
A kind of atmospheric and vacuum distillation unit reclaims the technique of lighter hydrocarbons, and its method is to use fore-running-air-distillation technique side
Case, just, often pushes up oil gas and delivers to absorption tower after compressor boosts, and absorbs light hydrocarbon component therein with often top is oily,
Then together sending into stabilizer with just top oil, tower top goes out liquefied petroleum gas product, goes out to stablize Petroleum at the bottom of tower；
Meanwhile, 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.As interim disclosed civilian in " oil refining design " 1996 volume 26 the 2nd
Chapter, 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 a large amount of
Light hydrocarbon component be dissolved in just in apex stone cerebrol, remaining small part light hydrocarbon component is dissolved in Chang Dingshi cerebrol,
Just, Chang Dingshi cerebrol send lighter hydrocarbons recovery unit after pump boosts (lighter hydrocarbons recovery unit can set single column flow process, double
Tower flow 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 method that new atmospheric and vacuum distillation unit reclaims 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 method that the first atmospheric and vacuum distillation unit reclaims lighter hydrocarbons, it is characterised in that: crude oil warp
Entering flash column after intensification, the tower top oil gas of flash column enters atmospheric tower middle and upper part, the tower base oil warp of flash column
Entering atmospheric tower bottom after intensification, the tower top oil gas of atmospheric tower often pushes up oil gas cold exchange device and normal top oil gas is low
Temperature condensing plant cooling, so that light hydrocarbon component all coagulates in oil phase in oil gas, the tower top oil gas warp of atmospheric tower
After cooling, temperature is 1～50 DEG C, and pressure is 0.005～0.1MPa, enters often top product and return tank, often
Being divided into two parts after the often top oil of top product and return tank is boosted, a part returns on atmospheric tower as backflow
Portion, remainder send lighter hydrocarbons recovery unit to separate dry gas (C1、C2), liquefied gas (C3、C4) and Petroleum
(C+ 5)。
The first atmospheric and vacuum distillation unit reclaims the method for lighter hydrocarbons and is technically characterized in that described normal top oil further
Coolant media used by gas condensation at low temperature equipment is chilled water, from the chilled water production unit of this device or other
Device.
The first atmospheric and vacuum distillation unit reclaims the method for lighter hydrocarbons and 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 first atmospheric and vacuum distillation unit reclaims the method for lighter hydrocarbons and is technically characterized in that described normal top oil further
Air cooling exchange device refers at least one in heat exchanger, air cooler and recirculated water cooling condenser.
The present invention provides the method that the second atmospheric and vacuum distillation unit reclaims lighter hydrocarbons, it is characterised in that: crude oil warp
Entering flash column after intensification, the tower top oil gas of flash column enters atmospheric tower middle and upper part, the tower base oil warp of flash column
Atmospheric tower bottom is entered after intensification, after the tower top oil gas of atmospheric tower often pushes up the cooling of primary oil air cooling exchange device,
Temperature is 35～120 DEG C, and pressure is 0.005～0.15MPa, enters often top return tank and separates, separates
Oil boosted after be divided into three parts, Part I as backflow return atmospheric tower top, Part II conduct
Naphtha product, Part III together with the oil gas that often top return tank separates often the two grades of oil gas cold exchange devices in top and
Often after the oil gas condensation at low temperature equipment condensation of two grades of top, temperature is 1～50 DEG C, and pressure is 0.005～0.1MPa,
Make light hydrocarbon component in oil gas all coagulate in oil phase, enter afterwards and often push up products pot, often the normal top of top products pot
Oil send lighter hydrocarbons recovery unit, separates dry gas (C at lighter hydrocarbons recovery unit1、C2), liquefied gas (C3、C4) and
Petroleum (C+ 5)。
The second atmospheric and vacuum distillation unit reclaims the method for lighter hydrocarbons and is technically characterized in that described normal top two further
Level coolant media used by oil gas condensation at low temperature equipment is chilled water, from this device chilled water production unit or
Other device.
The second atmospheric and vacuum distillation unit reclaims the method for 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 0.005～0.15MPa.
The second atmospheric and vacuum distillation unit reclaims the method for lighter hydrocarbons and 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 second atmospheric and vacuum distillation unit reclaims the method for lighter hydrocarbons and is technically characterized in that described Chang Dingyi further
Level oil gas cold exchange device and the often two grades of oil gas cold exchange devices in top refer to heat exchanger, air cooler and recirculated water cooling condenser
In at least one.
Atmospheric and vacuum distillation unit of the present invention reclaims the method for lighter hydrocarbons and 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) present invention can be under conditions of ensureing atmospheric and vacuum distillation unit routine operation, by using condensation at low temperature
Method, improves the absorbability of Petroleum, and at the beginning of making, in the oil gas of normal top, light hydrocarbon component can be the most molten to tower top stone
In cerebrol, thus it is sent to lighter hydrocarbons recovery unit through pump, the lighter hydrocarbons in crude oil can be reclaimed easily.
2) at present atmospheric and vacuum distillation unit reclaims the main two schemes of lighter hydrocarbons (" compressor scheme " and " first
Evaporate tower pressure boosting operation scheme ") in, " primary distillation tower pressure boosting operation scheme " energy consumption is higher (higher than the present invention program
About 0.2-0.5kgoe/t crude oil), " compressor scheme " one-time investment equipment maintenance cost high, dynamic is high, account for
Ground is many, operator are many, processes Processing High-sulfur High-Acidity Crude Oils especially, higher to material, the performance requirement of compressor,
Investment is bigger, and equipment maintenance cost is the highest, and compressor electricity consumption is many, and energy consumption is high (higher than the present invention program
About 0.04-0.07kgoe/t crude oil).Use the inventive method, without pressure boosting operation, be increased without compressor,
Capable of reducing energy consumption, reduce investment outlay, save operating cost.
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 method flow schematic diagram that the first atmospheric and vacuum distillation unit of the present invention reclaims lighter hydrocarbons.
Fig. 2 is the method flow schematic diagram that the second atmospheric and vacuum distillation unit of the present invention reclaims lighter hydrocarbons.
Reference shown in figure is:
1-flash column, 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 grades
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, and 16-inhales
Receiving tower, 17-desorber, 18-stabilizer, 19-stablizes return tank of top of the tower.
Detailed description of the invention
As it is shown in figure 1, Fig. 1 is the method that the first atmospheric and vacuum distillation unit reclaims lighter hydrocarbons.Crude oil is through heating up
Rear entrance flash column 1, the tower top oil gas of flash column 1 enters the middle and upper part of atmospheric tower 3, at the bottom of the tower of flash column 1
Oil enters the bottom of atmospheric tower 3 after atmospheric pressure kiln 2 heats up, and the tower top oil gas of atmospheric tower 3 the most often pushes up oil
After air cooling exchange device 4 and the often condensation of top oil gas condensation at low temperature equipment 5, temperature is 1-50 DEG C, and pressure is gauge pressure
0.005-0.1MPa, enters often top product and return tank 6, under normal circumstances, often top product and backflow afterwards
The gas outlet of tank 6 often pushes up product without gas emissions, the often top oil often pushing up product and return tank 6 and returns
Being divided into two parts after stream oil pump 7 boosting, a part returns the top of atmospheric tower 3, remainder as backflow
Enter lighter hydrocarbons recovery unit, be introduced into feed surge tank 15, after through absorption tower 16, desorber 17, stable
Tower 18 and stablize return tank of top of the tower 19, separates dry gas (C1、C2), liquefied gas (C3、C4) and Petroleum (C+5).
The first atmospheric and vacuum distillation unit described reclaims in the method for lighter hydrocarbons, 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.
The first atmospheric and vacuum distillation unit described reclaims in the method for lighter hydrocarbons, often top oil gas condensation at low temperature equipment 5
Chilled water used is from system share engineering.
As in figure 2 it is shown, Fig. 2 is the method that the second atmospheric and vacuum distillation unit reclaims 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, temperature after heat exchange cooling
For 35-120 DEG C, pressure is gauge pressure 0.005-0.15MPa, enters often top return tank 9 and separates, often pushes up
Being divided into two parts after the oil that return tank 9 separates often top reflux pump 10 boosting, a part often returns as backflow
Pressing the top of tower 3, together with the oil gas that another part separates with normal top return tank 9, often two grades of top oil gas is cold changes
After equipment 11 and the often two grades of oil gas condensation at low temperature equipment 12 in top, temperature is 1-50 DEG C, and pressure is gauge pressure
0.005-0.1MPa, enters often top products pot 13, under normal circumstances, often pushes up the gas outlet of products pot 13
Discharge without gas, often send lighter hydrocarbons recovery list after often top oil often top product oil pump 14 boosting of top products pot 13
Unit.
Described the second atmospheric and vacuum distillation unit reclaims in the method for lighter hydrocarbons, and often the temperature of top return tank 9 is
35-120 DEG C, pressure is gauge pressure 0.005-0.15MPa.
Described the second atmospheric and vacuum distillation unit reclaims in the method for lighter hydrocarbons, and often the temperature of top products pot 13 is
1-50 DEG C, pressure is gauge pressure 0.005-0.1MPa.
Described the second atmospheric and vacuum distillation unit reclaims in the method for lighter hydrocarbons, and often the two grades of oil gas condensation at low temperature in top set
Standby chilled water used by 12 is from system share engineering.
Claims (9)
1. the method that an atmospheric and vacuum distillation unit reclaims lighter hydrocarbons, it is characterised in that: crude oil enters after heating up
Flash column, the tower top oil gas of flash column enters atmospheric tower middle and upper part, and the tower base oil of flash column enters after heating up
Atmospheric tower bottom, the tower top oil gas of atmospheric tower often pushes up oil gas cold exchange device and often pushes up oil gas condensation at low temperature equipment
After condensation, temperature is 1～50 DEG C, and pressure is 0.005～0.1MPa, makes light hydrocarbon component in oil gas all coagulate
Often in the oil of top, enter often top product and return tank afterwards, after often the often top oil of top product and return tank is boosted
Being divided into two parts, a part returns to atmospheric tower top as backflow, and remainder send lighter hydrocarbons recovery unit to separate
Dry gas, liquefied gas and Petroleum.
A kind of atmospheric and vacuum distillation unit the most according to claim 1 reclaims the method for lighter hydrocarbons, and its feature exists
In: the coolant media used by the oil gas condensation at low temperature equipment of described normal top is chilled water, from the chilled water of this device
Production unit or other device.
A kind of atmospheric and vacuum distillation unit the most according to claim 1 reclaims the method for lighter hydrocarbons, and its feature exists
In: the temperature of described normal top product and return tank is 1～50 DEG C, and pressure is gauge pressure 0.005～0.1MPa.
A kind of atmospheric and vacuum distillation unit the most according to claim 1 reclaims the method for lighter hydrocarbons, and its feature exists
In: described normal top oil gas cold exchange device refers at least one in heat exchanger, air cooler and recirculated water cooling condenser.
5. the method that an atmospheric and vacuum distillation unit reclaims lighter hydrocarbons, it is characterised in that: crude oil enters after heating up
Flash column, the tower top oil gas of flash column enters atmospheric tower middle and upper part, and the tower base oil of flash column enters after heating up
Atmospheric tower bottom, after the tower top oil gas of atmospheric tower often pushes up primary oil air cooling exchange device partial condensation, temperature is
35～120 DEG C, pressure is 0.005～0.15MPa, enters often top return tank and separates, and the oil separated is through rising
Being divided into three parts after pressure, Part I returns to atmospheric tower top as backflow, and Part II produces as Petroleum
Product, Part III is the often two grades of oil gas cold exchange devices in top and often top two together with the oil gas that often top return tank separates
After level oil gas condensation at low temperature equipment condensation, temperature is 1～50 DEG C, and pressure is 0.005～0.1MPa, makes in oil gas
Light hydrocarbon component all coagulates in often top oil, enters afterwards and often pushes up products pot, and often the oil phase of top products pot send lighter hydrocarbons
Recovery unit, separates dry gas, liquefied gas and Petroleum at lighter hydrocarbons recovery unit.
A kind of atmospheric and vacuum distillation unit the most according to claim 5 reclaims the method for lighter hydrocarbons, and its feature exists
In: the coolant media used by the oil gas condensation at low temperature equipment of two grades of described normal top is chilled water, cold from this device
Matchmaker's water production unit or other device.
A kind of atmospheric and vacuum distillation unit the most according to claim 5 reclaims the method for lighter hydrocarbons, and its feature exists
In: the temperature of described normal top return tank is 35～120 DEG C, and pressure is gauge pressure 0.005～0.15MPa.
A kind of atmospheric and vacuum distillation unit the most according to claim 5 reclaims the method for lighter hydrocarbons, and its feature exists
In: the temperature of described normal top products pot is 1～50 DEG C, and pressure is gauge pressure 0.005～0.1MPa.
A kind of atmospheric and vacuum distillation unit the most according to claim 5 reclaims the method for lighter hydrocarbons, and its feature exists
In: described normal top primary oil air cooling exchange device and the often two grades of oil gas cold exchange devices in top refer to heat exchanger, air cooler
With at least one in recirculated water cooling condenser.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510016671.1A CN105885936A (en) | 2015-01-07 | 2015-01-07 | Method for recycling light hydrocarbon with atmospheric and vacuum distillation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510016671.1A CN105885936A (en) | 2015-01-07 | 2015-01-07 | Method for recycling light hydrocarbon with atmospheric and vacuum distillation device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105885936A true CN105885936A (en) | 2016-08-24 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510016671.1A Pending CN105885936A (en) | 2015-01-07 | 2015-01-07 | Method for recycling light hydrocarbon with atmospheric and vacuum distillation device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108865213A (en) * | 2018-07-13 | 2018-11-23 | 佛山市三水区精联自动化设备有限公司 | A kind of vacuum flash stabilising arrangement |
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| CN1343756A (en) * | 2000-09-16 | 2002-04-10 | 中国石化集团茂名石油化工公司 | Process for recovering light hydrocarbon for ordinary-pressure or depressurized distilling equipment |
| CN101376068A (en) * | 2008-09-17 | 2009-03-04 | 天津大学 | Atmospheric vacuum distillation method and apparatus with vacuum flash vaporizer |
| CN203625316U (en) * | 2013-10-29 | 2014-06-04 | 中国石油化工股份有限公司 | Oilfield light hydrocarbon separating device |
-
2015
- 2015-01-07 CN CN201510016671.1A patent/CN105885936A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1343756A (en) * | 2000-09-16 | 2002-04-10 | 中国石化集团茂名石油化工公司 | Process for recovering light hydrocarbon for ordinary-pressure or depressurized distilling equipment |
| CN101376068A (en) * | 2008-09-17 | 2009-03-04 | 天津大学 | Atmospheric vacuum distillation method and apparatus with vacuum flash vaporizer |
| CN203625316U (en) * | 2013-10-29 | 2014-06-04 | 中国石油化工股份有限公司 | Oilfield light hydrocarbon separating device |
Non-Patent Citations (2)
| Title |
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| 严錞等: "常减压蒸馏装置加工国外原油时采用初馏塔或闪蒸塔方案的探讨", 《石油炼制与化工》 * |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108865213A (en) * | 2018-07-13 | 2018-11-23 | 佛山市三水区精联自动化设备有限公司 | A kind of vacuum flash stabilising arrangement |
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Application publication date: 20160824 |