CN107285984A - The combination process that a kind of gas fractionation unit is expanded production and saved - Google Patents
The combination process that a kind of gas fractionation unit is expanded production and saved Download PDFInfo
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- CN107285984A CN107285984A CN201610222331.9A CN201610222331A CN107285984A CN 107285984 A CN107285984 A CN 107285984A CN 201610222331 A CN201610222331 A CN 201610222331A CN 107285984 A CN107285984 A CN 107285984A
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- tower
- depropanizing
- propylene rectification
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- chilled water
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Oil, Petroleum & Natural Gas (AREA)
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- Separation By Low-Temperature Treatments (AREA)
Abstract
The combination process expanded production and saved the invention discloses a kind of gas fractionation, the combination process is separated the liquefied gas raw material of the C5 containing C2 using gas fractionation unit, the gas fractionation unit includes depropanizing tower, dethanizer and the propylene rectification tower being sequentially connected, and depropanizing tower intermediate reboiler and propylene rectification tower intermediate reboiler are also respectively provided with depropanizing tower and propylene rectification tower；The cold public work of gas fractionation unit uses 5 15 DEG C of chilled water.The technique of the present invention by setting intermediate reboiler respectively on depropanizing tower and propylene rectification tower, use the technological means such as chilled water reduction depropanizing tower, dethanizer, propylene rectification tower operating pressure, under conditions of the tower body diameter and tower internals of various towers is not changed, the treating capacity increase 40 60% of gas fractionation unit is realized.In addition, the technique can reduce the potential temperature of the hot public work needed for device, and therefore reduce energy consumption.
Description
Technical field
The present invention relates to petrochemical enterprise gas fractionation technical field, in particular it relates to which a kind of gas fractionation unit expands
Production and the combination process of energy-conservation.
Background technology
Gas fractionation unit is the after-treatment device of the device product liquefied gas such as oil plant catalytic cracking, and its main task is
The propylene that there is Important Economic to be worth in liquefied gas is separated, using the raw material as polypropylene plant, while obtaining byproduct carbon two
Component, propane and carbon four, light dydrocarbon component.More than domestic gas fractionation unit using three towers (mainly by depropanizing tower, dethanizer and
Propylene rectification tower constitute) or four tower process flows (mainly by depropanizing tower, dethanizer, propylene rectification tower and depentanizer group
Into), wherein four-column process flow is, for further separation of carbon four, light dydrocarbon blending ingredients, to obtain the component of carbon four, to be used as MTBE devices
Raw material.
Currently, because refinery catalytic cracking unit generally uses producing more propylene scheme, or because oil refining apparatus totally adds
The raising of work amount so that gas fractionation unit processing capacity increase, therefore, faces Revamping problem.Gas fractionation unit needs
Implement Revamping by new device or to existing apparatus to adapt to new production status, wherein, most oil plants tend to
Revamping is implemented to original device.Use High Efficient Column Internals such as high-efficient tower plate more traditional fractionating column Revamping, efficiently fill out
Material etc. replaces existing tower internals, although this expands treating capacity, needs substantial amounts of equipment investment.
The energy consumption of gas fractionation unit is mainly the consumption of hot public work, due to depropanizing tower tower reactor boil again potential temperature compared with
Height, the hot public work of most gas depropanizing towers uses 0.4MPa steam, causes plant energy consumption higher.Partial depropanizer column with
100-120 DEG C of heat medium water is thermal source, reduces energy consumption level.Dethanizer, propylene rectification tower and depentanizer reboiler heat are public
With using atmospheric circulating heat medium water engineering more.There is researcher to propose that catalysis top recycle oil can be depropanizing tower and dethanizer, third
Alkene rectifying column, depentanizer reboiler provide thermal source, and insufficient section is supplemented by atmospheric circulating heat medium water, and this drops to a certain extent
The low energy consumption level of device.
Although researcher expands production to gas fractionation unit and reducing energy consumption proposes some schemes, in reply device processing
Amount expands, and also there are certain potentiality in terms of reduction gas fractionation unit energy consumption.
The content of the invention
In order in the case where not changing existing depropanizing tower, dethanizer, propylene rectification tower tower body diameter, improve gas
The treating capacity of fractionating device simultaneously saves energy consumption, the combination process expanded production and saved the invention provides a kind of gas fractionation unit.
A kind of combination process expanded production and saved the invention provides gas fractionation, the combination process is filled using gas fractionation
Liquefied gas raw material of the separation containing C2-C5 is put, the gas fractionation unit includes depropanizing tower, the dethanizer and third being sequentially connected
Depropanizing tower feed preheater, depropanizing tower overhead condenser and depropanizing tower bottom of towe are provided with alkene rectifying column, depropanizing tower
It is provided with deethanizer overhead condenser and deethanization tower bottom reboiler, propylene rectification tower and sets on reboiler, dethanizer
There are propylene rectification tower overhead condenser and propylene rectification tower tower bottom reboiler；The cold public work of the gas fractionation unit is adopted
With 5-15 DEG C of chilled water；
Wherein, depropanizing tower intermediate reboiler and propylene rectification tower are also respectively provided with depropanizing tower and propylene rectification tower
Intermediate reboiler；
The gas fractionation unit also includes refrigeration unit, and the refrigeration unit includes refrigeration plant and chilled water booster pump,
Chilled water is produced by refrigeration plant, and point two-way, enters propylene rectification tower overhead condenser all the way after being pressurized through chilled water booster pump, another
Road enters deethanizer overhead condenser, mixes afterwards, and the temperature of mixed chilled water is between 10-12 DEG C.
The combination process of the present invention does not change existing depropanizing tower, dethanizer, propylene rectification tower tower body diameter, realizes gas
Body fractionating device treating capacity increases 40-60%.The hot public work that device is consumed can be by 110-130 DEG C traditional of heating agent
Water, or 110-140 DEG C of hot logistics, or 0.4MPa steam, and 70-100 DEG C of heat medium water, are all changed to use 60-90 DEG C
Heat medium water.New technology have enlargement gas fractionating device treating capacity and reduction device needed for hot public work potential temperature it is excellent
Point.
Brief description of the drawings
By the way that exemplary embodiment of the invention is described in more detail with reference to accompanying drawing, it is of the invention above-mentioned and its
Its purpose, feature and advantage will be apparent.
Fig. 1 shows a kind of technological process of conventional gas fractionation unit.
Fig. 2 shows the gas point of the preferred embodiment of the present invention being improved for the technological process shown in Fig. 1
The combination process flow that distillation unit is expanded production and saved.
Fig. 3-5 respectively illustrates two kinds of depropanizing tower, dethanizer and the propylene rectification tower of embodiment 1 and comparative example
The hydraulics demand diameter distribution of operating mode, transverse axis N is the number of plates, and longitudinal axis d is tower diameter.
Description of reference numerals
1- liquefied gas raw material 2- depropanizing tower tower overhead gases
3- depropanizing tower overhead reflux 4- depropanizing tower overhead products
5- depropanizing towers bottom of towe boils return logistics 6- depropanizing tower tower bottom products again
7- dethanizers feed 8- deethanizer overhead gas
9- deethanizer overheads backflow 10- deethanizer overheads
11- dethanizers bottom of towe boils return logistics 12- dethanizer tower bottom products again
13- propylene rectification tower tower overhead gas 14- propylene rectification tower overhead refluxes
15- propylene rectification tower overhead product 16- propylene rectification tower bottom of towe boils return logistics again
17- propylene rectification tower tower bottom product 18- depropanizing towers
19- depropanizing tower feed preheater 20- depropanizing tower overhead condensers
21- depropanizing tower return tank of top of the tower 22- depropanizing tower tower bottom reboilers
23- depropanizing tower product booster pump 24- dethanizers
25- deethanizer overhead condenser 26- deethanizer overhead return tanks
27- dethanizer tower bottom reboiler 28- propylene rectification towers
29- propylene rectification tower overhead condenser 30- propylene rectification tower return tank of top of the tower
Extraction logistics is boiled again in the middle of 31- propylene rectification tower tower bottom reboiler 32- depropanizing towers
Return logistics 34- depropanizing tower intermediate reboilers are boiled in the middle of 33- depropanizing towers again
Boiled again in the middle of 35- propylene rectification towers and boil return logistics again in the middle of extraction logistics 36- propylene rectification towers
37- propylene rectification tower intermediate reboiler 38- chilled waters
39- is pressurized chilled water 40- propylene rectification tower condensing refrigerant water
The condensation of 41- propylene rectification towers returns to chilled water 42- dethanizer condensing refrigerant water
The condensation of 43- dethanizers returns to chilled water chilled water of 44-
The condensation of 45- depropanizing tower condensing refrigerant water 46- depropanizing towers returns to chilled water
47- returns to refrigeration plant chilled water 48- refrigeration plants
49- chilled water booster pumps
Embodiment
The preferred embodiment of the present invention is more fully described below with reference to accompanying drawings.
The technological process of existing gas fractionation unit is as shown in figure 1, depropanizing tower therein 18, propylene rectification tower 28
Operating pressure is between 1.8-2.2MPa, and the operating pressure of dethanizer 24 is between 2.5-2.8MPa；Each tower of device is cold
Public work is using conventional recirculated water.The present invention is improved on this basis, and the cold public affairs of each tower are used as by using chilled water
Tower operating pressure is reduced with engineering, intermediate reboiler, optimization depropanizing tower and propylene are set on depropanizing tower, propylene rectification tower
The feeding temperature of rectifying column, so as to expand depropanizing tower treating capacity and reduce the potential temperature of hot public work needed for depropanizing tower.Institute
Stating combination process can realize that gas fractionation unit treating capacity increases 40-60%.
Specifically, as shown in Fig. 2 the combination process expanded production and saved the invention provides a kind of gas fractionation, this is combined
Technology utilization gas fractionation unit separates the liquefied gas raw material containing C2-C5, and the gas fractionation unit is de- including what is be sequentially connected
Depropanizing tower feed preheater 19, de- third are provided with propane tower 18, dethanizer 24 and propylene rectification tower 28, depropanizing tower 18
Deethanizer overhead condenser 25 is provided with alkane column overhead condenser 20 and depropanizing tower tower bottom reboiler 22, dethanizer 24
With dethanizer tower bottom reboiler 27, propylene rectification tower overhead condenser 29 and propylene rectification tower are provided with propylene rectification tower 28
Tower bottom reboiler 31；The cold public work of the gas fractionation unit uses 5-15 DEG C of chilled water；
Wherein, depropanizing tower intermediate reboiler 34 and propylene are also respectively provided with depropanizing tower 18 and propylene rectification tower 28
Rectifying column intermediate reboiler 37；The gas fractionation unit also includes refrigeration unit, and the refrigeration unit includes the He of refrigeration plant 48
Chilled water booster pump 49, chilled water is produced by refrigeration plant 48, point two-way after being pressurized through chilled water booster pump 49, and propylene essence is entered all the way
Column overhead condenser 29 is evaporated, another road enters deethanization overhead condenser 25, mixed afterwards, the temperature of mixed chilled water is situated between
Between 10-12 DEG C.
In the present invention, the liquefied gas raw material refers to the desulfurization liquefied petroleum gas of the devices such as catalytic cracking, delayed coking.
Preferably, in the combination process, the chilled water of gas fractionation unit uses lithium bromide refrigerating.
Preferably, in the combination process, chilled water of the said temperature between 10-12 DEG C is again split into two-way, one
Road enters depropanizing tower overhead condenser 20, and another road is returned after being mixed with the chilled water that depropanizing tower overhead condenser 20 is exported
Refrigeration plant 48, the temperature for returning to the chilled water of refrigeration plant 48 is 15 DEG C.
Preferably, in the combination process, the cold public work of gas fractionation unit is used after chilled water, depropanizing tower
18 operating pressure is controlled in 0.8-1.2MPa.
Preferably, in the combination process, the cold public work of gas fractionation unit is used after chilled water, dethanizer
24 operating pressure is controlled in 1.2-1.8MPa.
Preferably, in the combination process, the cold public work of gas fractionation unit is used after chilled water, propylene rectifying
The operating pressure of tower 28 is controlled in 0.8-1.2MPa.
Preferably, in the combination process, it is provided with after depropanizing tower intermediate reboiler 34, controls on the depropanizing tower 18
The load for making operating mode depropanizing tower intermediate reboiler 34 of expanding production accounts for the 10- of the load of base operation condition depropanizing tower tower bottom reboiler 22
30%.
Preferably, in the combination process, depropanizing tower intermediate reboiler 34 is located in the middle part of the stripping section of depropanizing tower 18.
Preferably, in the combination process, the thermal source of depropanizing tower intermediate reboiler 34 is by temperature between 60-90 DEG C
Heat medium water provide.
Preferably, in the combination process, set on the propylene rectification tower 28 after propylene rectification tower intermediate reboiler 37,
The expand production load of operating mode propylene rectification tower intermediate reboiler 37 of control accounts for the load of base operation condition propylene rectification tower tower bottom reboiler 31
10-20%.
Preferably, in the combination process, propylene rectification tower intermediate reboiler 37 is located at the stripping section of propylene rectification tower 28
Middle part.
Preferably, in the combination process, the thermal source of propylene rectification tower intermediate reboiler 37 by temperature between 60-90 DEG C it
Between heat medium water provide.
Preferably, in the combination process, the feeding temperature of depropanizing tower 18 is optimized, control depropanizing tower 18 enters material temperature
Degree is between 50-70 DEG C.Wherein, heating agent of the thermal source of depropanizing tower feed preheater 19 by temperature between 60-90 DEG C
Water is provided.
A preferred embodiment of the invention, as shown in Fig. 2 except above-mentioned three fractionating columns, overhead condensations
Device, tower bottom reboiler, intermediate reboiler and refrigeration plant etc., gas fractionation unit also includes：It is depropanizing tower return tank of top of the tower 21, de-
Ethane tower return tank of top of the tower 26, propylene rectification tower top return tank 30 and depropanizing tower product booster pump 23；Wherein, liquefied gas raw material
1 enters the middle part of depropanizing tower 18 after depropanizing tower feed preheater 19 and heat medium water heat exchange, and depropanizing tower tower overhead gas 2 is through de-
After propane column overhead condenser 20 is condensed, into depropanizing tower return tank of top of the tower 21, depropanizing tower overhead product 4 is through depropanization
Tower overhead booster pump 23 enters dethanizer 24 after being pressurized；Extraction logistics 32 is boiled in the middle of depropanizing tower again through in depropanizing tower
Between reboiler 34 boil again after return the stripping section of depropanizing tower 18 middle part；Depropanizing tower tower base stream part is through depropanizing tower bottom of towe
Reboiler 22 returns to the bottom of towe of depropanizing tower 18 after boiling again, and remainder is used as the carrying device of depropanizing tower tower bottom product 6；
Deethanizer overhead gas 8 enters back into deethanizer overhead return tank 26 after being condensed through deethanizer overhead condenser 25
In, part backflow, remainder is used as the carrying device of deethanizer overhead 10；Deethanizer bottoms stream part is through de-
Ethane tower tower tower bottom reboiler 27 returns to the bottom of towe of depropanizing tower 24 after boiling again, and dethanizer tower bottom product 12 enters propylene rectification tower
28；
Propylene rectification tower tower overhead gas 13 enters back into propylene rectification tower tower top after being condensed through propylene rectification tower overhead condenser 29
In return tank 30, part backflow, remainder is as the carrying device of propylene rectification tower overhead product 15, in the middle of propylene rectification tower
Boil after extraction logistics 35 is boiled again through propylene rectification tower intermediate reboiler 37 and returned in the middle part of the stripping section of depropanizing tower 28 again, propylene rectifying
Tower tower base stream part returns to the bottom of towe of depropanizing tower 28 after being boiled again through propylene rectification tower tower bottom reboiler 31, and remainder is used as third
The carrying device of alkene rectifying tower bottom product 17；
In addition, being provided with refrigeration water station 48 on device, chilled water 38 is divided into two-way after being pressurized through chilled water booster pump 49：The
Propylene rectification tower condensing refrigerant water 40 enters propylene rectification tower overhead condenser 29, the second road dethanizer condensing refrigerant water all the way
42 enter deethanizer overhead condenser 25, and propylene rectification tower condensation returns to chilled water 41 and returns to chilled water with dethanizer condensation
43 mixing；The chilled water is again broken down into two-way：First via depropanizing tower condensing refrigerant water 45 enters depropanizing tower overhead condenser
20, depropanizing tower condensation returns after chilled water 46 is mixed with the second tunnel and returns to refrigeration plant 48.
All feed preheaters, intermediate reboiler and the tower bottom reboiler thermal source of the device are circulation heat medium water.
The present invention is described in detail below by embodiment, but the present invention should not be limited by the examples.
Embodiment 1
The present embodiment is used for the combination process for illustrating that the gas fractionation unit of the present invention is expanded production and saved.
This example is adjusted using 300,000 tons/year of gas fractionation units of certain petroleum chemical enterprise, and raw material is de- for catalytic cracking unit
Sulphur liquefied gas, flow is 36.0t/h, and its composition is shown in Table 1.The diameter of depropanizing tower, dethanizer and propylene rectification tower is respectively
2200mm, 1600mm, 3800mm, the number of plates are respectively 50,30 and 230.
Table 1
| Component | Content mol% | Component | Content mol% |
| Ethane+ethene | 0.5 | Propylene | 43.0 |
| Propane | 5.5 | N-butene | 6.5 |
| Isobutene | 12.5 | Butane | 5.0 |
| Maleic | 6.0 | Iso-butane | 12.0 |
| Pentane | 1.00 | Anti- butylene | 8.0 |
The concrete technology flow process of the present embodiment is as shown in Figure 2.
In this example, Process Quality Control index is：C4-C5≤0.1mol% in depropanizing tower overhead product, depropanizing tower
C2-C3≤0.1mol% in tower bottom product；C2 in C3≤0.1mol% in deethanizer overhead, dethanizer tower bottom product
≤ 0.1mol%；Propylene in propane≤0.05mol% in propylene rectification tower tower overhead, propylene rectification tower tower bottom product≤
0.1mol%.
Additionally, it is provided two kinds of operating modes, are contrasted by table 2-3 key indexs, the superiority of the present embodiment is verified.
Operating mode one is the refinery gas fractionating device present situation technological process, as shown in Figure 1.
Operating mode two is the operating mode of the present embodiment.
Table 2
| Parameter | Unit | Operating mode one | Operating mode two |
| Depropanizing tower feeding temperature | ℃ | 75 | 60 |
| Depropanizing tower operating pressure | MPa | 1.95 | 1.10 |
| Depropanizing tower tower top temperature | ℃ | 47 | 27 |
| Depropanizing tower column bottom temperature | ℃ | 107 | 83 |
| Dethanizer operating pressure | MPa | 2.65 | 1.70 |
| Deethanizer overhead temperature | ℃ | 44 | 25 |
| Dethanizer column bottom temperature | ℃ | 64 | 43 |
| Propylene rectification tower feeding temperature | ℃ | 65 | 43 |
| Propylene rectification tower operating pressure | MPa | 1.95 | 1.0 |
| Propylene rectification tower tower top temperature | ℃ | 47 | 33 |
| Propylene rectification tower column bottom temperature | ℃ | 61 | 20 |
| Chilled water feed temperature | ℃ | / | 5 |
| Chilled water return water temperature | ℃ | / | 15 |
Table 3
| Parameter | Unit | Operating mode one | Operating mode two |
| Treating capacity increases ratio | % | 0 | 55 |
| Depropanizing tower feed preheater load | M kCal | 1.00 | 0.95 |
| Depropanizing tower tower bottom reboiler load | M kCal | 3.40 | 4.00 |
| Depropanizing tower overhead condenser duty | M kCal | 3.20 | 4.80 |
| Depropanizing tower intermediate reboiler load | M kCal | / | 0.60 |
| Dethanizer tower bottom reboiler load | M kCal | 1.50 | 1.75 |
| Deethanizer overhead condenser load | M kCal | 1.30 | 1.40 |
| Propylene rectification tower tower bottom reboiler load | M kCal | 13.40 | 17.00 |
| Propylene rectification tower overhead condenser duty | M kCal | 13.60 | 18.80 |
| Propylene rectification tower intermediate reboiler load | M kCal | / | 1.50 |
| 0.4MPa steam consumptions | t/h | 6.5 | / |
| Heating agent water consumption | t/h | 800 | 1250 |
| Recirculated water/refrigeration water consumption | t/h | 1800 | 2600 |
Compared to operating mode one, the engineering of operating mode two, which changes content, to be included：
Newly-built refrigeration plant, chilled water increase pump and respective lines and lagging facility；
Increase overhead condenser, the heat-transfer surface of tower bottom reboiler of depropanizing tower, dethanizer and propylene rectification tower respectively
Product；
Increase depropanizing tower, the intermediate reboiler of propylene rectification tower newly respectively.
Fig. 3-5 is that the hydraulics of depropanizing tower, dethanizer and each column plate of propylene rectification tower under both the above operating mode is needed
Seek diameter distribution profile.Fig. 3-5 shows that operating mode two can effectively adjust each tower gas-liquid load distribution, rationally avoid because treating capacity increases
Caused liquid flooding possible greatly and flooding, realize that gas fractionation unit is expanded production.
Further, since the operating pressure reduction of depropanizing tower, dethanizer and propylene rectification tower, three tower reboilers are consumed
Hot public work temperature reduction, therefore, it is possible to all by 60-90 DEG C heat medium water substitute, eliminate depropanization in former operating mode
110-130 DEG C of heat medium water of tower consumption, or 110-140 DEG C of hot logistics, or 0.4MPa steam, and 70-100 DEG C of heating agent
Water.
The preferred embodiment of the present invention is described in detail above in association with accompanying drawing, still, the present invention is not limited to above-mentioned reality
The detail in mode is applied, in the range of the technology design of the present invention, a variety of letters can be carried out to technical scheme
Monotropic type, these simple variants belong to protection scope of the present invention.
It is further to note that each particular technique feature described in above-mentioned embodiment, in not lance
In the case of shield, can be combined by any suitable means, in order to avoid unnecessary repetition, the present invention to it is various can
The combination of energy no longer separately illustrates.
In addition, various embodiments of the present invention can be combined randomly, as long as it is without prejudice to originally
The thought of invention, it should equally be considered as content disclosed in this invention.
Claims (9)
1. the combination process that a kind of gas fractionation is expanded production and saved, it is characterised in that the combination process utilizes gas fractionation unit
The liquefied gas raw material containing C2-C5 is separated, the gas fractionation unit includes depropanizing tower (18), the dethanizer being sequentially connected
(24) depropanizing tower feed preheater (19), depropanizing tower tower top and propylene rectification tower (28), are provided with depropanizing tower (18)
Deethanizer overhead condenser (25) is provided with condenser (20) and depropanizing tower tower bottom reboiler (22), dethanizer (24)
With dethanizer tower bottom reboiler (27), propylene rectification tower overhead condenser (29) and propylene are provided with propylene rectification tower (28)
Rectifying column tower bottom reboiler (31), the cold public work of the gas fractionation unit uses 5-15 DEG C of chilled water；
Wherein, depropanizing tower intermediate reboiler (34) and third are also respectively provided with depropanizing tower (18) and propylene rectification tower (28)
Alkene rectifying column intermediate reboiler (37)；
The gas fractionation unit also includes refrigeration unit, and the refrigeration unit includes refrigeration plant (48) and chilled water booster pump
(49), chilled water is produced by refrigeration plant (48), and point two-way, enters propylene rectification tower tower all the way after being pressurized through chilled water booster pump (49)
Condenser (29) is pushed up, another road enters deethanizer overhead condenser (25), mixed afterwards, the temperature of mixed chilled water is situated between
Between 10-12 DEG C.
2. combination process according to claim 1, wherein, the refrigerant that the chilled water is used is lithium bromide.
3. combination process according to claim 1, wherein, in refrigeration unit, the mixed chilled water is divided again
For two-way, all the way into depropanizing tower overhead condenser (20), the system that another road is exported with depropanizing tower overhead condenser (20)
Refrigeration plant (48) is returned to after cold water mix, the temperature for returning to the chilled water of refrigeration plant (48) is 15 DEG C.
4. combination process according to claim 1, wherein, the cold public work of the gas fractionation unit uses chilled water
Afterwards, the operating pressure of depropanizing tower (18) is controlled in 0.8-1.2MPa；The operating pressure of dethanizer (24) is controlled in 1.2-
1.8MPa；The operating pressure of propylene rectification tower (28) is controlled in 0.8-1.2MPa.
5. combination process according to claim 1, wherein, set after depropanizing tower intermediate reboiler (34), control is expanded production
The load of operating mode depropanizing tower intermediate reboiler (34) accounts for the 10- of base operation condition depropanizing tower tower bottom reboiler (22) load
30%.
6. combination process according to claim 1 or 5, wherein, the depropanizing tower intermediate reboiler (34) is located at de- third
In the middle part of the stripping section of alkane tower (18)；Preferably, the thermal source of depropanizing tower intermediate reboiler (34) by temperature between 60-90 DEG C
Heat medium water provide.
7. combination process according to claim 1, wherein, set after propylene rectification tower intermediate reboiler (37), control is expanded
Production operating mode propylene rectification tower intermediate reboiler (37) load accounts for the 10- of base operation condition propylene rectification tower tower bottom reboiler (31) load
20%.
8. the combination process according to claim 1 or 7, wherein, the propylene rectification tower intermediate reboiler (37) is located at third
In the middle part of the stripping section of alkene rectifying column (28)；Preferably, propylene rectification tower intermediate reboiler (37) thermal source by temperature between 60-90 DEG C
Between heat medium water provide.
9. combination process according to claim 1, wherein, the feeding temperature of optimization depropanizing tower (19) controls depropanization
The feeding temperature of tower (18) is between 50-70 DEG C；Preferably, the thermal source of depropanizing tower feed preheater (19) by temperature between
Heat medium water between 60-90 DEG C is provided.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108147941A (en) * | 2017-12-22 | 2018-06-12 | 石家庄鼎盈化工股份有限公司 | Liquefied gas component separation of alkane and olefin system and separation method |
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