CN220724051U - Petroleum atmospheric and vacuum distillation device - Google Patents
Petroleum atmospheric and vacuum distillation device Download PDFInfo
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- CN220724051U CN220724051U CN202322243417.8U CN202322243417U CN220724051U CN 220724051 U CN220724051 U CN 220724051U CN 202322243417 U CN202322243417 U CN 202322243417U CN 220724051 U CN220724051 U CN 220724051U
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- 239000003208 petroleum Substances 0.000 title claims abstract description 22
- 238000005292 vacuum distillation Methods 0.000 title claims abstract description 19
- 238000010438 heat treatment Methods 0.000 claims abstract description 61
- 238000004821 distillation Methods 0.000 claims abstract description 40
- 238000010992 reflux Methods 0.000 claims description 125
- 238000000605 extraction Methods 0.000 claims description 98
- 239000000463 material Substances 0.000 claims description 29
- 238000005086 pumping Methods 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 6
- 238000012546 transfer Methods 0.000 claims description 6
- 239000010779 crude oil Substances 0.000 abstract description 17
- 238000005194 fractionation Methods 0.000 abstract description 14
- 230000008901 benefit Effects 0.000 abstract description 7
- 230000009466 transformation Effects 0.000 abstract 1
- 239000007791 liquid phase Substances 0.000 description 43
- 239000007789 gas Substances 0.000 description 36
- 239000012071 phase Substances 0.000 description 32
- 239000003921 oil Substances 0.000 description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 21
- 150000003839 salts Chemical class 0.000 description 15
- 238000000034 method Methods 0.000 description 14
- 238000005265 energy consumption Methods 0.000 description 12
- 238000004064 recycling Methods 0.000 description 12
- 239000000047 product Substances 0.000 description 11
- 230000006837 decompression Effects 0.000 description 10
- 239000003502 gasoline Substances 0.000 description 9
- 239000007788 liquid Substances 0.000 description 9
- 230000000694 effects Effects 0.000 description 8
- 230000008569 process Effects 0.000 description 8
- 238000002844 melting Methods 0.000 description 7
- 230000008018 melting Effects 0.000 description 7
- 230000009467 reduction Effects 0.000 description 7
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- 238000007670 refining Methods 0.000 description 6
- 239000000126 substance Substances 0.000 description 5
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 238000004134 energy conservation Methods 0.000 description 4
- 239000000284 extract Substances 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 239000007864 aqueous solution Substances 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000011033 desalting Methods 0.000 description 3
- 239000003350 kerosene Substances 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- 239000011552 falling film Substances 0.000 description 2
- 229910017053 inorganic salt Inorganic materials 0.000 description 2
- 230000010354 integration Effects 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000002407 reforming Methods 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 238000009835 boiling Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000010408 film Substances 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model provides a petroleum atmospheric and vacuum distillation device, which comprises a primary distillation tower, a negative pressure tower, an atmospheric tower and a vacuum tower which are sequentially connected, wherein the tops of the atmospheric tower and the vacuum tower are respectively connected with an atmospheric tower condenser and a vacuum tower condenser, the lower part of the negative pressure tower is connected with a negative pressure tower reboiler, the hot side outlet of the negative pressure tower reboiler is respectively connected with the atmospheric tower condenser and the vacuum tower condenser through heat exchange pipelines, and the atmospheric tower condenser and the vacuum tower condenser are respectively connected with the inlet of the negative pressure tower reboiler through heat supply pipelines; this application increases the negative pressure tower in the front of the atmospheric tower, has increased atmospheric tower throughput, reduces atmospheric tower heating furnace load, has improved the fractionation precision, and the effectual crude oil utilization ratio that has improved has reduced energy loss, increases the pull-out rate of device, has provided an atmospheric tower and has expanded energy transformation, excavates the new way of efficiency-increasing energy-conserving, increases the economic benefits of device.
Description
Technical Field
The application relates to the technical field of chemical equipment, in particular to a petroleum atmospheric and vacuum distillation device.
Background
Atmospheric and vacuum distillation is the first process of petroleum refining, crude oil after desalination and dehydration is cut into various petroleum fractions in an atmospheric and vacuum device, and because main equipment of the process comprises a primary distillation tower (or flash distillation tower), an atmospheric heating furnace, an atmospheric tower, a vacuum heating furnace and a vacuum tower, the process is called a three-stage distillation process flow of two-furnace three-tower for short.
The normal pressure heating furnace and the decompression heating furnace are collectively called a heating furnace, the heating furnace is a part with relatively high energy consumption for heating the petroleum distillate among the distillation towers, and the quality, the yield and the economic benefit of the subsequent devices are directly related to the technical level of the atmospheric and decompression distillation.
The energy conservation of the existing atmospheric and vacuum devices is to design and optimize a crude oil heat exchange network by adopting a pinch point analysis principle, match energy of various grades, utilize the utilized waste heat, increase the mass transfer coefficient of a heat exchanger through the heat exchange network, improve the energy recycling efficiency, and finally, some energy is wasted; the global oil refining capability continues to increase, and the oil refining capability reaches 55 hundred million tons/year in 2025, and the world oil refining capability in the next few years is expected to increase beyond the requirement, and a large excess of energy will be at risk, so that energy conservation and consumption reduction are still necessary for saving oil refining cost.
The applicant searches the prior art in detail, and searches the closest comparison file as follows:
comparative document 1: the technical scheme is provided by the petroleum atmospheric and vacuum distillation process with the application number of 201110102559.1, wherein a raw material inlet of a vacuum distillation tower or/and an atmospheric tower is connected with a tube side of a dividing wall type heat exchanger, a shell side inlet of the dividing wall type heat exchanger is connected with a molten salt heating furnace, a shell side outlet of the dividing wall type heat exchanger is connected with a melting tank, and the molten salt heating furnace is connected with the melting tank; adding mixed inorganic salt powder particles into a melting tank, introducing high-pressure steam or electricity into the melting tank, melting the mixed inorganic salt powder particles into liquid, when the melting temperature reaches 180 ℃, starting a molten salt circulating pump to force liquid phase circulation of molten salt, conveying the molten salt to a molten salt heating furnace for heating, controlling the temperature of the molten salt at an outlet of the molten salt furnace or the inlet temperature of molten salt flow of a dividing wall type heat exchanger to be 350-530 ℃, conveying the molten salt to the dividing wall type heat exchanger for heating petroleum flow to 360-440 ℃, and returning the molten salt to the melting tank; petroleum flows out of the dividing wall type heat exchanger and enters an atmospheric tower or a vacuum tower; the method has low coking probability, and can improve heating temperature and extraction rate of the distillation tower.
In the scheme, a heating furnace in front of a distillation tower in the prior art is changed into a dividing wall type heat exchanger for exchanging heat between molten salt and petroleum, and the heating heat of the petroleum is changed into a dividing wall type heat exchanger; the new partition wall type heat exchanger for exchanging heat between molten salt and petroleum needs to be added in the whole system, the utilization rate of the existing heating furnace is 0, the new device is introduced, the investment rate of the whole equipment can be higher, in the technical scheme, the primary distillation tower, the normal pressure tower and the vacuum tower are sequentially connected, the normal pressure tower bottom oil enters the molten salt heat exchanger to be heated to 360-440 ℃ and then enters the vacuum tower, the load of the molten salt heat exchanger is not reduced, and the heat at the tops of the normal pressure tower and the vacuum tower is not utilized, so that the energy consumption is not reduced compared with the prior art.
Therefore, a new technical solution is needed to solve the above technical problems.
Disclosure of Invention
The application provides a petroleum atmospheric and vacuum distillation device, including primary tower, atmospheric tower, the vacuum tower that connects gradually, atmospheric tower and the top of vacuum tower are connected with atmospheric tower condenser, vacuum tower condenser respectively, be provided with the negative pressure tower between primary tower, the atmospheric tower, the lower part of negative pressure tower is connected with the negative pressure tower reboiler, and the hot side export of negative pressure tower reboiler is connected with atmospheric tower condenser, vacuum tower condenser respectively through heat exchange pipeline, and atmospheric tower condenser, vacuum tower condenser are connected with the inlet connection of negative pressure tower reboiler through heating pipeline respectively.
As a preferable scheme, an atmospheric tower heat pump is arranged on a heating pipeline at the top of the atmospheric tower condenser, and a vacuum tower heat pump is arranged on a heating pipeline at the top of the vacuum tower condenser.
As a preferable scheme, the top of the negative pressure tower is connected with a negative pressure tower condenser, the negative pressure tower condenser is connected with a negative pressure tower reflux device, the negative pressure tower condenser is connected with a first heat exchange pipeline, and the first heat exchange pipeline is connected with a second heat exchange pipeline.
As a preferred scheme, the top of primary tower is connected with primary tower reflux unit, primary tower reflux unit includes primary tower top pipeline that the primary tower top set up, primary tower condenser, primary tower reflux drum, primary tower reflux pump have set gradually on the primary tower top pipeline, be connected with the primary tower through primary tower reflux pipeline on the primary tower top pipeline at primary tower reflux pump rear portion.
As a preferred scheme, one side of the negative pressure tower is provided with a heat exchange condenser, the heat exchange condenser is connected with a primary tower condenser through a primary tower heat exchange pipeline I, a primary tower heat pump is arranged on the primary tower heat exchange pipeline I, the heat exchange condenser is also connected with the primary tower condenser through a primary tower heat exchange pipeline II, and a primary tower pump body is arranged on the primary tower heat exchange pipeline II.
As a preferred scheme, negative pressure tower reflux unit includes negative pressure tower reflux drum, negative pressure tower reflux drum is connected with the top of negative pressure tower through negative pressure tower top extraction pipeline, be provided with the negative pressure tower condenser on the negative pressure tower top extraction pipeline, the bottom of negative pressure tower reflux drum is connected with the well upper portion of negative pressure tower through negative pressure tower reflux pipeline, the bottom of negative pressure tower reflux drum still is equipped with the component extraction pipeline, negative pressure tower condenser is connected with the extraction pipeline.
As a preferable scheme, the extraction pipeline is provided with a negative pressure tower heat pump.
As a preferable scheme, one side of the negative pressure tower is connected with a negative pressure stripping tower through a negative pressure tower side line, one side of the negative pressure stripping tower is filled with steam, the top of the negative pressure stripping tower is connected with one side of the negative pressure tower through a negative pressure stripping top pipeline, and the bottom of the negative pressure stripping tower is provided with a component extraction pipeline I.
As a preferable scheme, the top of the atmospheric tower is connected with an atmospheric tower reflux device, the atmospheric tower reflux device comprises an atmospheric tower reflux tank, the atmospheric tower reflux tank is connected with the top of the atmospheric tower through an atmospheric tower top extraction pipeline, an atmospheric tower condensation device is connected on the atmospheric tower top extraction pipeline, the bottom of the atmospheric tower reflux tank is connected with an atmospheric tower material extraction pipeline, an atmospheric tower reflux pipeline is connected on the atmospheric tower material extraction pipeline, and the atmospheric tower reflux pipeline is connected with the middle upper part of the atmospheric tower.
As a preferable scheme, the atmospheric tower condensation device adopts an atmospheric tower condenser, the atmospheric tower condenser is connected with a negative pressure tower reboiler through a heating pipeline, an atmospheric tower heat pump is arranged on the heating pipeline, and a hot side outlet of the negative pressure tower reboiler is connected with the atmospheric tower condenser through the heat exchange pipeline.
As a preferred scheme, atmospheric tower condensation equipment includes atmospheric tower condenser and the air cooler of parallelly connected setting, be provided with the valve before atmospheric tower condenser and the air cooler respectively, the atmospheric tower condenser passes through the heating pipeline and is connected with the negative pressure tower reboiler, be provided with the atmospheric tower heat pump on the heating pipeline, the hot side export of negative pressure tower reboiler passes through the heat transfer pipeline is connected with the atmospheric tower condenser.
As a preferable scheme, the rear part of the atmospheric tower condenser is provided with a secondary atmospheric tower condenser, the secondary atmospheric tower condenser is connected with a circulation loop, the circulation loop is provided with a heat pump, and the rear part of the heat pump is provided with a heat exchanger on the circulation loop.
As a preferable scheme, the atmospheric tower is connected with the atmospheric stripping tower through an atmospheric tower side line, the atmospheric stripping tower is connected with the atmospheric tower through an atmospheric tower reflux side line, the atmospheric stripping tower is filled with steam, and one side of the atmospheric stripping tower is connected with an atmospheric stripping tower extraction pipeline.
As a preferable scheme, the side line of the atmospheric tower, the reflux side line of the atmospheric tower and the extraction pipeline of the atmospheric stripping tower are respectively provided with three.
As a preferred scheme, vacuum pumping device is provided with at the vacuum tower top, vacuum pumping device includes the vacuum tower buffer tank, and the top of vacuum tower buffer tank is connected with the top of vacuum tower through vacuum tower top extraction pipeline, is provided with the vacuum tower condenser on the vacuum tower top extraction pipeline, and the top and the bottom of vacuum tower buffer tank are connected with vacuum pumping pipeline and vacuum tower buffer tank extraction pipeline respectively.
As a preferable scheme, the vacuum tower condenser is connected with a vacuum tower reboiler through a heating pipeline, a vacuum tower heat pump is arranged on the heating pipeline, and a hot side outlet of the vacuum tower reboiler is connected with the vacuum tower condenser through a heat exchange pipeline.
As a preferable scheme, one side of the vacuum tower is respectively connected with a first side reduction line, a second side reduction line and a third side reduction line, wherein the first side reduction line and the second side reduction line are respectively connected with the vacuum tower through a vacuum tower reflux pipeline.
As a preferable scheme, the bottom of the vacuum tower is connected with a bottom-reduced residual oil extraction pipeline.
As a preferable scheme, a reflux tank and a delivery pump are arranged on the heat exchange pipeline.
The application has the following advantages:
1. the negative pressure tower is added in front of the atmospheric tower, so that the treatment capacity of the atmospheric tower is increased, the load of the atmospheric tower or an atmospheric tower heating furnace is reduced, the fractionation precision is improved, the crude oil utilization rate is effectively improved, the energy loss is reduced, the extraction rate of the device is increased, a new way for expanding and reforming the atmospheric tower is provided, the efficiency and energy conservation are improved, and the economic benefit of the device is increased; the load of the normal pressure tower or the heating furnace of the normal pressure tower is reduced, so that scaling and pressure drop of crude oil in a heat exchange network are reduced, the heat exchange efficiency is improved, the product variety can be increased, the influence of crude oil carrying water on the normal pressure tower is relieved, and the method is suitable for ultra-light oil operation;
2. the method comprises the steps of carrying out heat cascade utilization on tower top steam of a primary distillation tower, a negative pressure tower, an atmospheric tower and a vacuum tower, upgrading and pressurizing the energy of the tower top steam of the primary distillation tower through a heat pump, then enabling the energy to enter the middle section of the negative pressure tower for backflow to consume the energy, condensing the energy into liquid water, introducing the liquid water into a primary distillation tower condenser at the tower top of the primary distillation tower through a pump for recycling, carrying out heat recycling on the tower top steam of the atmospheric tower and the vacuum tower, adopting a heat pump refrigeration working medium to take heat, namely upgrading gasified media through the heat pump, carrying out heat exchange and pressurizing, enabling the steam to reach a certain pressure, introducing a negative pressure tower reboiler to consume the energy after saturation, and respectively introducing the liquid water into the atmospheric tower condenser and the vacuum tower condenser through the pump for heating and recycling; leading out and utilizing the tower top steam of the negative pressure tower, and reasonably utilizing the low temperature of the tower top; further achieving the effects of reducing energy consumption, recycling heat and improving fractionation efficiency;
3. the normal pressure tower exchanges heat with the stripping tower, so that the load of the reduced pressure heating furnace is reduced, the fractionation precision is improved, the crude oil utilization rate is effectively improved, and the energy loss is reduced;
4. the modification is carried out on the original equipment, new equipment is not required to be introduced, the existing equipment is only required to be added, the utilization rate of the equipment is high, and the investment is relatively small;
5. reasonably distributing the processing load of the atmospheric and vacuum system, carrying out heat integration, optimizing the heat exchange flow, and reducing the energy consumption so as to adapt to the requirements of large-scale devices and diversified processed petroleum;
6. the circulating water is saved, and the heat of the discharged atmosphere is reduced;
7. the utility model changes the traditional oil refining process, is beneficial to the recovery of the waste heat energy of the device, is convenient for production and operation, can effectively improve the extraction rate, reduce the energy loss and the heat loss due to good mass transfer effect, and has the effect of saving investment; the whole has the functions of reducing energy consumption, recycling heat and improving fractionation efficiency.
Drawings
FIG. 1 is a schematic structural view of the present application;
1. primary distillation tower 2, negative pressure tower 3, normal pressure tower 4 and vacuum tower
5. Primary tower bottom pipeline 6, primary tower delivery pump 7 and primary tower material conveying condenser
8. Negative pressure tower bottom pipeline 9, normal pressure heating furnace 10 and normal pressure tower bottom pipeline
11. Vacuum heating furnace 12, atmospheric tower delivery pump 13 and bottom-reduced residual oil extraction pipeline
14. Vacuum tower delivery pump 15, vacuum tower delivery condenser 16 and negative pressure stripping tower
17. Negative pressure tower reboiler 18, heating pipeline 19, heat exchange pipeline 20, primary tower reflux drum
21. Primary tower top line 22, primary tower condenser 23, extraction line 24, primary tower heat pump
27. Heat exchange condenser 28, primary tower reflux pump 29, primary tower reflux line
30. Negative pressure tower reflux drum 31, negative pressure tower top extraction pipeline 32, negative pressure tower condenser
33. Negative pressure tower reflux pipeline 34, negative pressure tower reflux pump 35 and component extraction pipeline
36. Negative pressure column side line 37, negative pressure stripping top line 38, component extraction line one
39. Atmospheric tower reflux drum 40, atmospheric tower top extraction line 41, atmospheric tower condenser
42. Atmospheric tower material extraction line 43, atmospheric tower reflux line 44, and atmospheric tower reflux pump
45. Atmospheric tower heat pump 46, reflux drum 47, transfer pump 48, and atmospheric stripper
49. First 50 of the side line of the atmospheric tower, first 51 of the side line of the atmospheric tower and third of the side line of the atmospheric tower
52. First reflux side line 53, second reflux side line 54, and third reflux side line
55. Extraction line one 56 and extraction line two of normal pressure stripping tower
57. Extraction line III 58, extraction pump 59 and buffer tank of vacuum tower of normal pressure stripping tower
60. Vacuum tower top extraction line 61, vacuum tower condenser 63, and vacuum line
64. Decompression tower buffer tank extraction pipeline 65, decompression tower delivery pump 66 and decompression tower heat pump
67. Minus one side line 68, minus two side lines 69, minus three side lines
70. Vacuum tower reflux line 71, electric desalting tank 72 and negative pressure tower heat pump
73. Heat exchange line one 74, condenser 75, primary tower heat exchange line one
76. Primary tower heat exchange pipeline II 77, primary tower pump body 78 and air cooler
79. Valve 80, heating furnace 81, secondary atmospheric tower condenser 82, and circulation loop
83. Heat pump 84, heat exchanger.
Detailed Description
The following describes the embodiment of the present utility model in detail with reference to fig. 1. It should be noted that the detailed description herein is presented for purposes of illustration and explanation only and is not intended to limit the utility model.
Embodiment one:
the application provides a petroleum atmospheric and vacuum distillation device, which comprises a primary distillation tower 1, a negative pressure tower 2, an atmospheric tower 3 and a vacuum tower 4 which are sequentially connected, wherein the bottom of the primary distillation tower 1 is connected with the middle upper part of the negative pressure tower 2 through a primary distillation tower bottom pipeline 5, a primary tower conveying pump 6 and a primary tower material conveying condenser 7 are sequentially arranged on the primary distillation tower bottom pipeline 5 between the primary distillation tower 1 and the negative pressure tower 2, the bottom of the negative pressure tower 2 is connected with the middle lower part of the atmospheric tower 3 through a negative pressure tower bottom pipeline 8, an atmospheric heating furnace 9 is arranged on the negative pressure tower bottom pipeline 8 and is used for heating materials in the tower kettle of the negative pressure tower 2, the bottom of the atmospheric tower 3 is connected with the vacuum tower 4 through an atmospheric tower bottom pipeline 10, a vacuum heating furnace 11 is arranged on the atmospheric tower bottom pipeline 10, the front part of the vacuum heating furnace 11 is provided with an atmospheric tower conveying pump 12 on an atmospheric tower bottom pipeline 10, the bottom of the vacuum tower 4 is connected with a bottom-reduced residual oil extraction pipeline 13, the bottom-reduced residual oil extraction pipeline 13 is provided with a vacuum tower conveying pump 14 and a vacuum tower conveying condenser 15, the lower part of the vacuum tower 2 is connected with a vacuum tower reboiler 17, during starting, heat is firstly provided for the vacuum tower reboiler 17 through steam and the like, the energy of the vacuum tower 2 is derived from the vacuum tower reboiler 17, the vacuum tower reboiler 17 adopts a circulating forced falling film reboiler or a forced circulating rising film reboiler, wherein the falling film reboiler has the advantages of low surface temperature, short material residence time and low process side line pressure, and is used for further preventing coking, optimizing production, adopting vacuum rectification operation from the technical aspect, reducing the boiling point of materials and reducing the occurrence of thermal degradation of the materials; the tops of the atmospheric tower 3 and the vacuum tower 4 are respectively connected with an atmospheric tower condenser 41 and a vacuum tower condenser 61, the hot side outlet of the vacuum tower reboiler 17 is respectively connected with the atmospheric tower condenser 41 and the vacuum tower condenser 61 through heat exchange pipelines 19, and the atmospheric tower condenser 41 and the vacuum tower condenser 61 are respectively connected with the inlet of the vacuum tower reboiler 17 through heat supply pipelines 18; after the gas phases at the tops of the atmospheric tower 3 and the vacuum tower 4 are respectively condensed by the atmospheric tower condenser 41 and the vacuum tower condenser 61, reflux and product extraction are carried out, the liquid phase in the vacuum tower reboiler 17 after heat exchange respectively enters the atmospheric tower condenser 41 and the vacuum tower condenser 61 through a hot side outlet of the vacuum tower reboiler 17 and a heat exchange pipeline 19, the materials flowing through the atmospheric tower condenser 41 and the vacuum tower condenser 61 in the heat exchange pipeline 19 are heated by utilizing the heat of the gas phases at the tops of the atmospheric tower 3 and the vacuum tower 4, and enter the inlet of the vacuum tower reboiler 17 after heat addition, and enter the next working cycle.
Preferably, the heat supply pipeline 18 at the top of the atmospheric tower condenser 41 is provided with the atmospheric tower heat pump 45, the heat supply pipeline 18 at the top of the vacuum tower condenser 61 is provided with the vacuum tower heat pump 66, materials heated by the atmospheric tower condenser 41 and the vacuum tower condenser 61 are compressed and heated by the atmospheric tower heat pump 45 and the vacuum tower heat pump 66, heat required by the negative pressure tower reboiler 17 is achieved, heat is not required to be continuously supplied to the negative pressure tower reboiler 17 through external steam, the heat utilization rate of the tops of the atmospheric tower 3 and the vacuum tower 4 is improved, and energy consumption is reduced.
According to the embodiment, the negative pressure tower 2 is added in front of the normal pressure tower 3, the traditional three-tower atmospheric and vacuum process is changed into a four-tower four-stage distillation process, so that the load of the normal pressure tower 3 or the normal pressure heating furnace 9 is reduced, meanwhile, the scaling and the pressure drop of crude oil in a heat exchange network are reduced, the heat exchange efficiency is improved, the product variety can be increased, the influence of crude oil carrying water on the normal pressure tower is relieved, the ultra-light oil operation is adapted, and the effects of reducing the energy consumption, recycling the heat and improving the fractionation efficiency are realized; this application can carry out the heat retrieval and utilization to atmospheric tower 3, the top of a tower steam of vacuum tower 4, carries out the heat extraction with different heat pump refrigerating medium respectively, if: water is used when the temperature is high, so that the pressurization is safe; when the temperature is low, methanol and R-13a are used for heat extraction, namely a heat pump is used for upgrading gasified media, heat exchange is carried out firstly, then pressure is increased, steam reaches a certain pressure, after saturation, energy is consumed by a negative pressure tower reboiler 17 which is introduced into a negative pressure tower 2, and condensed liquid water is respectively introduced into an atmospheric tower condenser 41 and a vacuum tower condenser 61 for recycling through pumps; thereby further achieving the effects of reducing energy consumption, recycling heat and improving fractionation efficiency.
Embodiment two:
the present embodiment specifically describes the preliminary distillation column 1, specifically:
the top of primary tower 1 is connected with primary tower reflux unit, primary tower reflux unit includes primary tower top pipeline 21 that primary tower 1 top set up, primary tower condenser 22, condenser 74, primary tower reflux drum 20, primary tower reflux pump 28 have set gradually on the primary tower top pipeline 21, be connected with primary tower 1 through primary tower reflux pipeline 29 on the primary tower top pipeline 21 at primary tower reflux pump 28 rear portion.
The gas phase at the top of the primary tower 1 enters the primary tower reflux tank 20 after being condensed by the primary tower condenser 22 and the condenser 74, one part of liquid phase in the primary tower reflux tank is refluxed to the primary tower 1 through the primary tower reflux pipeline 29, and the other part of liquid phase is extracted into light gasoline through the primary tower top pipeline 21.
Embodiment III:
the negative pressure column 2 is specifically described in this embodiment, specifically:
the top of negative pressure tower 2 is provided with negative pressure tower reflux unit, negative pressure tower reflux unit includes negative pressure tower reflux drum 30, negative pressure tower reflux drum 30 is connected with the top of negative pressure tower 2 through negative pressure tower top extraction pipeline 31, be provided with negative pressure tower condenser 32 on the negative pressure tower top extraction pipeline 31, the bottom of negative pressure tower reflux drum 30 is connected with the well upper portion of negative pressure tower 2 through negative pressure tower reflux drum 33, is provided with negative pressure tower reflux pump 34 on the negative pressure tower reflux drum 33, the bottom of negative pressure tower reflux drum 30 still is equipped with component extraction pipeline 35, preferably includes naphtha extraction pipeline and aqueous solution extraction pipeline, is used for extracting naphtha and aqueous solution respectively, negative pressure tower condenser 32 is connected with extraction pipeline 23, be provided with negative pressure tower heat pump 72 on the extraction pipeline 23, with the overhead vapor extraction of negative pressure tower 2 utilized, the rational utilization overhead low temperature heat, for example: the heat of the part of steam with the temperature of 60-70 ℃ is changed into hot water with the temperature of 70-80 ℃ through the 72-stage boost of the negative pressure tower heat pump, and the heat can be used for heating and preserving heat; the gas phase at the top of the negative pressure tower 2 is condensed by a negative pressure tower condenser 32 and then enters a negative pressure tower reflux tank 30, a part of liquid phase in the negative pressure tower reflux tank 30 flows back to the negative pressure tower 2 through a negative pressure tower reflux pipeline 33, and a part of liquid phase is extracted into naphtha and/or aqueous solution through a component extraction pipeline 35.
Preferably, in order to further utilize the heat of the top of the negative pressure tower 2, the negative pressure tower condenser 32 is connected with a first heat exchange line 73, and the first heat exchange line 73 is connected with a heat exchange line 19; the gas phase at the top of the negative pressure tower 2 is condensed by a negative pressure tower condenser 32 and then enters a negative pressure tower reflux tank 30, one part of liquid phase of the negative pressure tower reflux tank 30 flows back to the negative pressure tower 2 through a negative pressure tower reflux pipeline 33, and the other part of liquid phase of the negative pressure tower reflux tank is used for extracting naphtha and/or water solution through a component extraction pipeline 35; the liquid phase after heat exchange in the negative pressure tower reboiler 17 enters the negative pressure tower condenser 32 through a hot side outlet of the negative pressure tower reboiler 17, a heat exchange pipeline 19 and a first heat exchange pipeline 73, the heat of the gas phase at the top of the negative pressure tower 2 is utilized to heat the material flowing in the negative pressure tower condenser 32 in the first heat exchange pipeline 73, and after the heated liquid phase is compressed and heated through the negative pressure tower heat pump 72, the vapor at the top of the negative pressure tower 2 is led out through a production pipeline 23 for utilization, and the low temperature heat at the top of the tower is reasonably utilized.
Further, in order to ensure the product quality and fractionation precision of the negative pressure tower 2, improve the flash point of the product and reduce the content of light components, one side of the negative pressure tower 2 is connected with the negative pressure stripping tower 16 through a negative pressure tower side line 36, one side of the negative pressure stripping tower 16 is filled with steam, the top of the negative pressure stripping tower 16 is connected with one side of the negative pressure tower 2 through a negative pressure stripping top line 37 as the power of the negative pressure stripping tower 16, a component extraction line I38 is arranged at the bottom of the negative pressure stripping tower 16, part of the material of the negative pressure tower 2 enters the negative pressure stripping tower 16 through the negative pressure tower side line 36 to be stripped, the gas phase at the top of the negative pressure stripping tower 16 enters the negative pressure tower 2 through a negative pressure stripping top line 37 to be distilled continuously, and the component extraction line I38 at the bottom of the negative pressure stripping tower 16 is used for extracting kerosene.
Further, in order to fully utilize the heat of the gas phase at the top of the primary distillation tower 1, a heat exchange condenser 27 is arranged at one side of the negative pressure tower 2, the primary distillation tower condenser 27 is connected with the primary tower condenser 22 through a primary distillation tower heat exchange pipeline I75, a primary tower heat pump 24 is arranged on the primary distillation tower heat exchange pipeline I75, the heat exchange condenser 27 is also connected with the primary tower condenser 22 through a primary distillation tower heat exchange pipeline II 76, and a primary tower pump body 77 is arranged on the primary distillation tower heat exchange pipeline II 76; the gas phase at the top of the primary tower 1 enters a primary tower reflux tank 20 after being condensed by a primary tower condenser 22 and a condenser 74, one part of liquid phase in the primary tower reflux tank is refluxed to the primary tower 1 through a primary tower reflux pipeline 29, and the other part of liquid phase is extracted into light gasoline through a primary tower top pipeline 21; the liquid phase at the output end of the heat exchange condenser 27 is conveyed to the primary tower condenser 22 through the primary tower pump body 77 for heat exchange, the material flowing through the primary tower condenser 22 in the primary tower heat exchange pipeline II 76 is heated by utilizing the heat of the gas phase at the top of the primary tower 1, and the heated liquid phase is further compressed and heated through the primary tower heat pump 24 and then enters the inlet of the heat exchange condenser 27 to provide heat for the middle-section reflux of the negative pressure tower 2.
Embodiment four:
the atmospheric tower 3 will be specifically described in this embodiment, specifically:
the top of the atmospheric tower 3 is connected with an atmospheric tower reflux device, the atmospheric tower reflux device comprises an atmospheric tower reflux tank 39, the atmospheric tower reflux tank 39 is connected with the top of the atmospheric tower 3 through an atmospheric tower top extraction pipeline 40, an atmospheric tower condensing device is connected on the atmospheric tower top extraction pipeline 40, the bottom of the atmospheric tower reflux tank 39 is connected with an atmospheric tower material extraction pipeline 42, an atmospheric tower reflux pipeline 43 is connected on the atmospheric tower material extraction pipeline 42, and the atmospheric tower reflux pipeline 43 is connected with the middle upper part of the atmospheric tower 3; an atmospheric tower reflux pump 44 is arranged on the atmospheric tower material extraction pipeline 42, and an atmospheric tower reflux pipeline 43 is connected to the atmospheric tower material extraction pipeline 42 at the rear part of the atmospheric tower reflux pump 44; the gas phase extracted from the top of the atmospheric tower 3 is cooled by the atmospheric tower condensing equipment and then enters the atmospheric tower reflux tank 39, a part of liquid phase of the atmospheric tower reflux tank 39 is refluxed to the atmospheric tower 3 through the atmospheric tower reflux pipeline 43, and a part of liquid phase of the atmospheric tower reflux tank is extracted into gasoline through the atmospheric tower substance extraction pipeline 42.
Preferably, the atmospheric tower condensation device adopts an atmospheric tower condenser 41, the atmospheric tower condenser 41 is connected with the negative pressure tower reboiler 17 through a heating pipeline 18, and an atmospheric tower heat pump 45 is arranged on the heating pipeline 18; the hot side outlet of the negative pressure tower reboiler 17 is connected with an atmospheric tower condenser 41 through a heat exchange pipeline 19, and a reflux tank 46 and a delivery pump 47 are arranged on the heat exchange pipeline 19; the gas phase at the top of the atmospheric tower 3 is cooled by an atmospheric tower condenser 41 and then enters an atmospheric tower reflux tank 39, a part of liquid phase of the atmospheric tower reflux tank 39 is refluxed to the atmospheric tower 3 through an atmospheric tower reflux pipeline 43, a part of liquid phase of the atmospheric tower reflux tank is used for extracting gasoline through an atmospheric tower substance extraction pipeline 42, the liquid phase in the negative pressure tower reboiler 17 after heat exchange enters the atmospheric tower condenser 41 for heat exchange through a hot side outlet of the negative pressure tower reboiler 17 and a heat exchange pipeline 19, the heat of the gas phase at the top of the atmospheric tower 3 is utilized for heating the material flowing through the atmospheric tower condenser 41 in the heat exchange pipeline 19, and the heated liquid phase atmospheric tower heat pump 45 is compressed and heated and then enters an inlet of the negative pressure tower reboiler 17 for heating the negative pressure tower reboiler 17 and then enters the next working cycle.
The embodiment also provides an additional form of atmospheric tower condensing equipment, which comprises an atmospheric tower condenser 41 and an air cooler 78 which are arranged in parallel, wherein the front parts of the atmospheric tower condenser 41 and the air cooler 78 are respectively provided with a valve 79, the atmospheric tower condenser 41 is connected with a negative pressure tower reboiler 17 through a heat supply pipeline 18, the heat supply pipeline 18 is provided with an atmospheric tower heat pump 45, the hot side outlet of the negative pressure tower reboiler 17 is connected with the atmospheric tower condenser 41 through a heat exchange pipeline 19, and the heat exchange pipeline 19 is provided with a reflux tank 46 and a conveying pump 47; the heat of the top of the atmospheric tower 3 is transmitted to the water cooling of the atmospheric tower condenser 41 and the air cooling of the air cooler 78 by the atmospheric tower condensing equipment, the gas phase of the top of the atmospheric tower 3 is condensed by the atmospheric tower condenser 41 and/or the air cooling device 78, the condensed gas phase enters the atmospheric tower reflux tank 39, a part of liquid phase of the atmospheric tower reflux tank 39 flows back to the atmospheric tower 3 through the atmospheric tower reflux pipeline 43, a part of liquid phase of the atmospheric tower reflux tank extracts gasoline through the atmospheric tower material extraction pipeline 42, the liquid phase of the negative pressure tower reboiler 17 after heat exchange enters the atmospheric tower condenser 41 through the hot side outlet of the negative pressure tower reboiler 17 and the heat exchange pipeline 19 for heat exchange, the material flowing through the atmospheric tower condenser 41 in the heat exchange pipeline 19 is heated by the heat of the gas phase of the top of the atmospheric tower 3, and the heated liquid phase of the atmospheric tower heat pump 45 enters the inlet of the negative pressure tower reboiler 17 for heat supply after compression and the temperature rise, and enters the next working cycle; the scheme fully utilizes the heat of the top of the atmospheric tower 3, saves circulating water and reduces the heat of the discharged atmosphere.
More preferably, the two types of atmospheric tower condensing apparatuses are provided with a secondary atmospheric tower condenser 81 at the rear part of the atmospheric tower condenser 41, the secondary atmospheric tower condenser 81 is connected with a circulation loop 82, the circulation loop 82 is provided with a heat pump 83, and the rear part of the heat pump 83 is provided with a heat exchanger 84 on the circulation loop 82, in this embodiment, two different heat pump upgrades are provided, one stage is a gas phase condensed by the atmospheric tower condenser 41, the heat thereof is used for heating the effluent liquid phase at the hot side outlet of the negative pressure tower reboiler 17, and then the heat is upgraded into steam with high pressure grade by the compressor of the atmospheric tower heat pump 45, and the steam enters the negative pressure tower reboiler 17 for providing heat for the negative pressure tower reboiler 17; the second stage is a gas phase condensed by the second-stage atmospheric tower condenser 81, the heat of the gas phase is utilized to heat the liquid phase in the circulation loop 82, then the heat pump 83 compresses and heats the liquid phase, and the heat compressed by the heat pump 83 is absorbed by the heat exchanger 84 to be used in other working procedures; for example: one is that the energy of 120 ℃ is reduced to 70 ℃ and is upgraded into steam with high pressure level by a compressor of the atmospheric tower heat pump 45, and the other is that the energy is recycled by a heat pump 83 and a heat exchanger 84 after the heat is condensed and released when the temperature of 70 ℃ is reduced to 40 ℃.
Further, in order to ensure the product quality and fractionation precision of the atmospheric tower 3, the product quality and flash point are ensured, the partial pressure of light components is reduced, and the extraction rate of crude oil is improved; the atmospheric tower 3 is connected with the atmospheric stripping tower 48 through an atmospheric tower side line, the atmospheric stripping tower 48 is connected with the atmospheric stripping tower 3 through an atmospheric tower reflux side line, steam is introduced into the atmospheric stripping tower 48, the steam provides power for the atmospheric stripping tower 48, one side of the atmospheric stripping tower 48 is connected with an atmospheric stripping tower extraction pipeline, the atmospheric stripping tower extraction pipeline extracts corresponding products, in the embodiment, the atmospheric tower is connected with the atmospheric stripping tower 48 through an atmospheric tower side line I49, an atmospheric tower side line II 50 and an atmospheric tower side line III 51, the atmospheric stripping tower 48 is respectively connected with the atmospheric stripping tower 3 through an atmospheric tower reflux side line I52, an atmospheric tower reflux side line II 53 and an atmospheric stripping tower reflux side line III 54, one side of the atmospheric stripping tower 48 is connected with an atmospheric stripping tower extraction pipeline I55, an atmospheric stripping tower extraction pipeline II 56 and an atmospheric stripping tower extraction pipeline III 57, the atmospheric stripping tower extraction pipeline I55, the atmospheric stripping tower extraction pipeline II 56 and the atmospheric stripping tower extraction pipeline III 57 are all provided with extraction pumps 58, and the diesel oil tower I55 extraction pipeline II and the atmospheric stripping tower extraction pipeline III 57 are used for heavy diesel oil extraction.
The atmospheric tower 3 is provided with 3 side products and 3 middle reflux streams so as to uniformly distribute the gas-liquid load of the whole tower and facilitate optimizing the heat exchange network of the whole device, and the surplus heat of the whole tower is recovered, and the whole tower is used for heating crude oil and generating steam; to ensure product quality and fractionation accuracy, the side stream product is provided with an atmospheric stripper 48.
Fifth embodiment:
the present embodiment describes the pressure reduction column 4, specifically:
the top of the pressure reducing tower 4Is provided with a vacuumizing device ， The vacuumizing device comprises a vacuum tower buffer tank 59, the top of the vacuum tower buffer tank 59 is connected with the top of the vacuum tower 4 through a vacuum tower top extraction pipeline 60, a vacuum tower condenser 61 is arranged on the vacuum tower top extraction pipeline 60, the top and the bottom of the vacuum tower buffer tank 59 are respectively connected with a vacuumizing pipeline 63 and a vacuum tower buffer tank extraction pipeline 64, and a vacuum tower conveying pump 65 is arranged on the vacuum tower buffer tank extraction pipeline 64; the vacuumizing device is used for pumping out the tower top gas of the vacuum tower 4 and ensuring the vacuum degree of the tower top; specifically, the gas phase at the top of the vacuum tower 4 enters the vacuum tower buffer tank 59 after being cooled by the vacuum tower condenser 61, the top of the vacuum tower buffer tank 59 is vacuumized, and the top of the vacuum tower buffer tank 59 is used for extracting top-reduced oil through the vacuum tower buffer tank extraction pipeline 64.
Preferably, the vacuum tower condenser 61 is connected with the negative pressure tower reboiler 17 through a heat supply pipeline 18, a vacuum tower heat pump 66 is arranged on the heat supply pipeline 18, the gas phase at the top of the vacuum tower 4 enters the vacuum tower buffer tank 59 after being cooled by the vacuum tower condenser 61, the top of the vacuum tower buffer tank 59 is vacuumized, the top of the vacuum tower buffer tank 59 extracts the top-reduced oil through a vacuum tower buffer tank extraction pipeline 64, the liquid phase in the negative pressure tower reboiler 17 after heat exchange enters the vacuum tower condenser 61 through a hot side outlet of the negative pressure tower reboiler 17 and a heat exchange pipeline 19 for heat exchange, the heat of the gas phase at the top of the vacuum tower 4 heats the material flowing through the vacuum tower condenser 61 through the heat exchange pipeline 19, and the heated liquid phase enters the inlet of the negative pressure tower reboiler 17 after being compressed and heated by the vacuum tower heat pump 66 for heat supply, and enters the next working cycle; the scheme fully utilizes the heat of the gas phase at the top of the vacuum tower 4, saves circulating water and reduces the heat discharged to the atmosphere.
One side of the pressure reducing tower 4 is respectively connected with a first side reducing line 67, a second side reducing line 68 and a third side reducing line 69, the first side reducing line 67, the second side reducing line 68 and the third side reducing line 69 are used for extracting different grades of lubricating oil according to different substances extracted from different crude oils, and the fuel type adopts different grades of wax oil and the like; wherein the reduced side line 67 and the reduced side line 68 are respectively connected with the vacuum tower 4 through a vacuum tower reflux line 70 ； The bottom of the vacuum tower 4 is connected with a bottom-reduced residual oil extraction pipeline 13.
The working principle of the application is as follows: crude oil enters an electric desalting tank 71 for desalting and dewatering, and the feeding temperature is 360-370 ℃; the desalted and dehydrated petroleum is heated by a heating furnace 80 and then enters a primary distillation tower 1, the top of the primary distillation tower 1 is provided with tower top reflux, primary distillation tower top gas and primary distillation tower light gasoline are pumped out, the bottom oil of the primary distillation tower 1 enters a negative pressure tower 2 after heat exchange, the top gas phase of the negative pressure tower 2 is pumped out and naphtha and/or water are extracted from the top of the negative pressure tower 2, side materials of the negative pressure tower 2 are stripped by a negative pressure stripping tower 16, component kerosene is extracted, a negative pressure tower reboiler 17 provides heat for the negative pressure tower 2, tower bottom oil at the bottom of the negative pressure tower 2 enters an atmospheric tower 3 after being heated by an atmospheric pressure heating furnace 9, atmospheric pressure tower 3 is pumped out of atmospheric pressure tower top gas and gasoline, the atmospheric pressure tower 3 is provided with 3 side lines, an atmospheric pressure stripping tower extraction pipeline I55, an atmospheric pressure stripping tower extraction pipeline II 56 and an atmospheric pressure stripping tower extraction pipeline III 57 respectively extract kerosene, light diesel and heavy diesel after stripping steam is stripped by an atmospheric pressure stripping tower 48; the bottom oil of the atmospheric tower 3 is gradually heated by a decompression heating furnace 11 and then enters a decompression tower 4, a vacuum pumping device is arranged at the top of the decompression tower 4, the top gas of the decompression tower 4 is pumped out, the vacuum degree of the top of the tower is kept, and top-reduced oil is extracted from the top of the decompression tower 4; the gas phase at the top of the primary distillation tower 1 enters a primary tower reflux tank 20 after being condensed by a primary tower condenser 22 and a condenser 74, part of liquid phase in the primary tower reflux tank is refluxed to the primary distillation tower 1 through a primary tower reflux pipeline 29, and the other part of liquid phase is extracted into light gasoline through a primary distillation tower top pipeline 21; the liquid phase at the output end of the heat exchange condenser 27 is conveyed to the primary tower condenser 22 through the primary tower pump body 77 for heat exchange, the material flowing through the primary tower condenser 22 in the primary tower heat exchange pipeline II 76 is heated by utilizing the heat of the gas phase at the top of the primary tower 1, and the heated liquid phase is further compressed and heated through the primary tower heat pump 24 and then enters the inlet of the heat exchange condenser 27 to provide heat for the middle section reflux of the negative pressure tower 2; the gas phase at the top of the negative pressure tower 2 enters the negative pressure tower reflux tank 30 after being condensed by the negative pressure tower condenser 32, a part of liquid phase of the negative pressure tower reflux tank 30 flows back to the negative pressure tower 2 through the negative pressure tower reflux pipeline 33, a part of liquid phase of the negative pressure tower reflux tank is used for extracting naphtha and/or water solution through the component extraction pipeline 35, the liquid phase in the negative pressure tower reboiler 17 after heat exchange enters the negative pressure tower condenser 32 for heat exchange through a hot side outlet of the negative pressure tower reboiler 17, a heat exchange pipeline 19 and a heat exchange pipeline one 73, the material flowing in the negative pressure tower condenser 32 in the heat exchange pipeline one 73 is heated by utilizing the heat of the gas phase at the top of the negative pressure tower 2, and after the heated liquid phase is compressed and heated by the negative pressure tower heat pump 72, the top steam of the negative pressure tower 2 is led out for use through the extraction pipeline 23, and the low temperature heat at the top of the tower is reasonably utilized; the gas phase at the top of the atmospheric tower 3 is cooled by an atmospheric tower condensing device and then enters an atmospheric tower reflux tank 39, a part of liquid phase of the atmospheric tower reflux tank 39 is refluxed to the atmospheric tower 3 through an atmospheric tower reflux pipeline 43, a part of liquid phase of the atmospheric tower reflux tank is used for extracting gasoline through an atmospheric tower substance extraction pipeline 42, the liquid phase in a negative pressure tower reboiler 17 after heat exchange enters an atmospheric tower condenser 41 for heat exchange through a hot side outlet of the negative pressure tower reboiler 17 and a heat exchange pipeline 19, the heat of the gas phase at the top of the atmospheric tower 3 is utilized for heating the material flowing in the atmospheric tower condenser 41 in the heat exchange pipeline 19, and the heated liquid phase atmospheric tower heat pump 45 is compressed and heated and then enters an inlet of the negative pressure tower reboiler 17 for heating the negative pressure tower reboiler 17 and then enters the next working cycle; the gas phase at the top of the vacuum tower 4 enters the vacuum tower buffer tank 59 after being cooled by the vacuum tower condenser 61, the top of the vacuum tower buffer tank 59 is vacuumized, top oil is extracted from the top of the vacuum tower buffer tank 59 through the vacuum tower buffer tank extraction pipeline 64, the liquid phase in the negative pressure tower reboiler 17 after heat exchange enters the vacuum tower condenser 61 for heat exchange through the hot side outlet of the negative pressure tower reboiler 17 and the heat exchange pipeline 19, the heat of the gas phase at the top of the vacuum tower 4 is utilized to heat the material flowing through the vacuum tower condenser 61 in the heat exchange pipeline 19, and the heated liquid phase enters the inlet of the negative pressure tower reboiler 17 after being compressed and heated by the vacuum tower heat pump 66, so as to supply heat to the negative pressure tower reboiler 17 and enter the next working cycle.
In summary, due to the adoption of the technical scheme, the utility model has the following advantages:
1. the negative pressure tower is added in front of the atmospheric tower, so that the treatment capacity of the atmospheric tower is increased, the load of the atmospheric tower or an atmospheric tower heating furnace is reduced, the fractionation precision is improved, the crude oil utilization rate is effectively improved, the energy loss is reduced, the extraction rate of the device is increased, a new way for expanding and reforming the atmospheric tower is provided, the efficiency and energy conservation are improved, and the economic benefit of the device is increased; the load of the normal pressure tower or the heating furnace of the normal pressure tower is reduced, so that scaling and pressure drop of crude oil in a heat exchange network are reduced, the heat exchange efficiency is improved, the product variety can be increased, the influence of crude oil carrying water on the normal pressure tower is relieved, and the method is suitable for ultra-light oil operation;
2. the method comprises the steps of carrying out heat cascade utilization on tower top steam of a primary distillation tower, a negative pressure tower, an atmospheric tower and a vacuum tower, upgrading and pressurizing the energy of the tower top steam of the primary distillation tower through a heat pump, then enabling the energy to enter a middle section of the negative pressure tower for backflow to consume energy, condensing the energy into liquid water, introducing the liquid water into a primary distillation tower condenser at the tower top of the primary distillation tower through a pump for cyclic utilization, carrying out heat recycling on the tower top steam of the atmospheric tower and the vacuum tower, respectively using different heat pump refrigeration working mediums (such as water when the temperature is high, pressurizing is safe, using methanol and R-13 a) for heat extraction when the temperature is low, namely upgrading gasified mediums through the heat pump, carrying out heat exchange and pressurizing after the steam reaches a certain pressure, introducing the negative pressure tower reboiler to consume the energy after saturation, and introducing the liquid water into the atmospheric tower condenser and the vacuum tower condenser for cyclic utilization through the pump respectively; leading out and utilizing the tower top steam of the negative pressure tower, and reasonably utilizing the low temperature of the tower top; further achieves the effects of reducing energy consumption, recycling heat and improving fractionation efficiency.
3. The normal pressure tower exchanges heat with the stripping tower, so that the load of the reduced pressure heating furnace is reduced, the fractionation precision is improved, the crude oil utilization rate is effectively improved, and the energy loss is reduced;
4. the modification is carried out on the original equipment, new equipment is not required to be introduced, the existing equipment is only required to be added, the utilization rate of the equipment is high, and the investment is relatively small;
5. reasonably distributing the processing load of the atmospheric and vacuum system, carrying out heat integration, optimizing the heat exchange flow, and reducing the energy consumption so as to adapt to the requirements of large-scale devices and diversified processed petroleum;
6. the circulating water is saved, and the heat of the discharged atmosphere is reduced;
7. the utility model changes the traditional oil refining process, is beneficial to the recovery of the waste heat energy of the device, is convenient for production and operation, can effectively improve the extraction rate, reduce the energy loss and the heat loss due to good mass transfer effect, and has the effect of saving investment; the whole has the functions of reducing energy consumption, recycling heat and improving fractionation efficiency.
The above devices, connection relationships, etc. which are not specifically described belong to the prior art, and the present utility model is not specifically described herein.
The preferred embodiments of the present application have been described in detail above with reference to the accompanying drawings, but the present application is not limited to the specific details of the foregoing embodiments, and various simple modifications may be made to the technical solutions of the present application within the scope of the technical concept of the present application, and all the simple modifications belong to the protection scope of the present application.
In addition, the specific features described in the foregoing embodiments may be combined in any suitable manner, and in order to avoid unnecessary repetition, various possible combinations of the present utility model are not described in detail.
Moreover, any combination of the various embodiments of the present application may be made without departing from the spirit of the present application, which is also to be considered as disclosed herein.
Claims (10)
1. The utility model provides a petroleum atmospheric and vacuum distillation device, includes preliminary distillation tower (1), atmospheric tower (3), vacuum tower (4) that connect gradually, the top of atmospheric tower (3) and vacuum tower (4) is connected with atmospheric tower condenser (41), vacuum tower condenser (61) respectively, a serial communication port, be provided with negative pressure tower (2) between preliminary distillation tower (1), atmospheric tower (3), the lower part of negative pressure tower (2) is connected with negative pressure tower reboiler (17), and the hot side export of negative pressure tower reboiler (17) is connected with atmospheric tower condenser (41), vacuum tower condenser (61) respectively through heat transfer pipeline (19), and atmospheric tower condenser (41), vacuum tower condenser (61) are connected with the inlet connection of negative pressure tower reboiler (17) through heating pipeline (18) respectively.
2. The atmospheric and vacuum distillation unit for petroleum according to claim 1, wherein the top of the negative pressure tower (2) is connected with a negative pressure tower condenser (32), the negative pressure tower condenser (32) is connected with a negative pressure tower reflux device, the negative pressure tower condenser (32) is connected with a first heat exchange pipeline (73), and the first heat exchange pipeline (73) is connected with a second heat exchange pipeline (19).
3. The petroleum atmospheric and vacuum distillation device according to claim 1, wherein a heat exchange condenser (27) is arranged on one side of the negative pressure tower (2), the heat exchange condenser (27) is connected with the primary tower condenser (22) through a primary tower heat exchange pipeline I (75), a primary tower heat pump (24) is arranged on the primary tower heat exchange pipeline I (75), the heat exchange condenser (27) is also connected with the primary tower condenser (22) through a primary tower heat exchange pipeline II (76), and a primary tower pump body (77) is arranged on the primary tower heat exchange pipeline II (76).
4. The petroleum atmospheric and vacuum distillation device according to claim 2, wherein the negative pressure tower reflux device comprises a negative pressure tower reflux tank (30), the negative pressure tower reflux tank (30) is connected with the top of the negative pressure tower (2) through a negative pressure tower top extraction pipeline (31), a negative pressure tower condenser (32) is arranged on the negative pressure tower top extraction pipeline (31), the bottom of the negative pressure tower reflux tank (30) is connected with the middle upper part of the negative pressure tower (2) through a negative pressure tower reflux pipeline (33), and the bottom of the negative pressure tower reflux tank (30) is also provided with a component extraction pipeline (35).
5. The atmospheric and vacuum distillation unit as claimed in claim 4, wherein the negative pressure tower condenser (32) is connected to a production line (23), and a negative pressure tower heat pump (72) is provided on the production line (23).
6. The atmospheric and vacuum distillation apparatus as claimed in claim 1, wherein the top of the atmospheric tower (3) is connected with an atmospheric tower reflux apparatus, the atmospheric tower reflux apparatus comprises an atmospheric tower reflux tank (39), the atmospheric tower reflux tank (39) is connected with the top of the atmospheric tower (3) through an atmospheric tower top extraction line (40), an atmospheric tower condensing device is arranged on the atmospheric tower top extraction line (40), an atmospheric tower material extraction line (42) is connected with the bottom of the atmospheric tower reflux tank (39), an atmospheric tower reflux line (43) is connected with the atmospheric tower material extraction line (42), and the atmospheric tower reflux line (43) is connected with the middle upper part of the atmospheric tower (3).
7. The atmospheric and vacuum distillation apparatus as claimed in claim 6, wherein the atmospheric tower condensing device employs an atmospheric tower condenser (41), the atmospheric tower condenser (41) is connected to a negative pressure tower reboiler (17) through a heating pipeline (18), and an atmospheric tower heat pump (45) is disposed on the heating pipeline (18).
8. The atmospheric and vacuum distillation apparatus as claimed in claim 6, wherein the atmospheric tower condensing device comprises an atmospheric tower condenser (41) and an air cooler (78) which are arranged in parallel, valves (79) are respectively arranged in front of the atmospheric tower condenser (41) and the air cooler (78), the atmospheric tower condenser (41) is connected with a negative pressure tower reboiler (17) through a heating pipeline (18), and an atmospheric tower heat pump (45) is arranged on the heating pipeline (18).
9. The atmospheric and vacuum distillation unit for petroleum according to claim 1, wherein the top of the vacuum tower (4) is provided with a vacuum pumping device, the vacuum pumping device comprises a vacuum tower buffer tank (59), the top of the vacuum tower buffer tank (59) is connected with the top of the vacuum tower (4) through a vacuum tower top extraction pipeline (60), a vacuum tower condenser (61) is arranged on the vacuum tower top extraction pipeline (60), and the top and the bottom of the vacuum tower buffer tank (59) are respectively connected with a vacuum pumping pipeline (63) and a vacuum tower buffer tank extraction pipeline (64).
10. A petroleum atmospheric and vacuum distillation unit as claimed in claim 9, wherein the vacuum column condenser (61) is connected to the negative pressure column reboiler (17) via a heating line (18), and the heating line (18) is provided with a vacuum column heat pump (66).
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