CN117700294A - Separation process and device for C four-C six petroleum hydrocarbon - Google Patents
Separation process and device for C four-C six petroleum hydrocarbon Download PDFInfo
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- CN117700294A CN117700294A CN202311579903.5A CN202311579903A CN117700294A CN 117700294 A CN117700294 A CN 117700294A CN 202311579903 A CN202311579903 A CN 202311579903A CN 117700294 A CN117700294 A CN 117700294A
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- 238000000926 separation method Methods 0.000 title claims abstract description 170
- 239000003209 petroleum derivative Substances 0.000 title claims abstract description 40
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 175
- AFABGHUZZDYHJO-UHFFFAOYSA-N 2-Methylpentane Chemical compound CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 claims abstract description 165
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 116
- 238000005262 decarbonization Methods 0.000 claims abstract description 50
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 60
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical group CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 claims description 54
- 229930195733 hydrocarbon Natural products 0.000 claims description 50
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 48
- 150000002430 hydrocarbons Chemical class 0.000 claims description 45
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 claims description 24
- 238000005261 decarburization Methods 0.000 claims description 17
- 239000004215 Carbon black (E152) Substances 0.000 claims description 16
- 239000001273 butane Substances 0.000 claims description 15
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 15
- 238000012546 transfer Methods 0.000 claims description 7
- 238000005265 energy consumption Methods 0.000 abstract description 18
- 238000002156 mixing Methods 0.000 abstract description 6
- 238000010992 reflux Methods 0.000 description 44
- 239000007789 gas Substances 0.000 description 40
- 239000000047 product Substances 0.000 description 38
- 230000000052 comparative effect Effects 0.000 description 24
- 238000000034 method Methods 0.000 description 21
- 239000000203 mixture Substances 0.000 description 17
- 238000001816 cooling Methods 0.000 description 13
- 239000003208 petroleum Substances 0.000 description 11
- 239000002994 raw material Substances 0.000 description 8
- 238000009826 distribution Methods 0.000 description 6
- -1 C 6 Hydrocarbon Chemical class 0.000 description 5
- 239000002918 waste heat Substances 0.000 description 5
- BDJOPCBWIOGONH-UHFFFAOYSA-N butane;2-methylbutane Chemical compound CCCC.CCC(C)C BDJOPCBWIOGONH-UHFFFAOYSA-N 0.000 description 4
- 238000004517 catalytic hydrocracking Methods 0.000 description 4
- 238000005194 fractionation Methods 0.000 description 4
- 230000005611 electricity Effects 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 238000002407 reforming Methods 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 238000003556 assay Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- JCCNYMKQOSZNPW-UHFFFAOYSA-N loratadine Chemical compound C1CN(C(=O)OCC)CCC1=C1C2=NC=CC=C2CCC2=CC(Cl)=CC=C21 JCCNYMKQOSZNPW-UHFFFAOYSA-N 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 230000003313 weakening effect Effects 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a separation process and a separation device of four-carbon to six-carbon petroleum hydrocarbon, and relates to the technical field of petrochemical industry. According to the invention, the first base tower in the four-tower sequential separation process of the decarbonization four-isopentane tower-n-pentane tower-isohexane tower is changed into the prefractionator, the second base tower is changed into the decarbonization four-tower, the third base tower is changed into the carbon five-component separation tower, and meanwhile, the third base tower and the fourth base tower are changed from original serial connection into parallel connection, so that the carbon four-to-carbon six-petroleum hydrocarbon is sequentially separated through the prefractionator, the decarbonization four-tower, the carbon five-component separation tower and the isohexane tower, the energy consumption of the four-to-carbon six-petroleum hydrocarbon separation process is greatly reduced, the middle distillate back mixing is reduced, the rectification efficiency is improved, and the separation of the carbon four-to-carbon six-petroleum hydrocarbon is effectively realized while the energy consumption is reduced.
Description
Technical Field
The invention relates to the technical field of petrochemical industry, in particular to a separation process and a separation device of four-carbon to six-carbon petroleum hydrocarbon.
Background
In the petroleum processing process, devices such as continuous reforming, hydrocracking and the like can generate a large amount of C four-C six petroleum hydrocarbon (C 4 ～C 6 ) The separation of the high-purity monomer is an important means for increasing the value of the product. The conventional four-to-six-carbon petroleum hydrocarbon separation process is four-tower sequential separation, and the process sequentially passes through a decarburization four-tower, an isopentane tower, a n-pentane tower and an isohexane tower to obtain butane (the concentration is more than or equal to 99 wt%), isopentane (the concentration is more than or equal to 95 wt%), n-pentane (the concentration is more than or equal to 99 wt%), isohexane (the concentration is more than or equal to 99 wt%), and n-hexane (the concentration is more than or equal to 99 wt%).
However, because the boiling points of the four-carbon to six-carbon petroleum hydrocarbons are close, the back mixing of intermediate components is serious, the energy consumption in the separation process is high, for example, a set of equipment with the treatment capacity of 40t/h generally consumes about 50t/h of steam with the treatment capacity of 0.5MPa, and the separation of the raw materials consumes 1.25t/h.
Therefore, there is a need to develop a process that can effectively separate four to six carbon petroleum hydrocarbons with low energy consumption.
Disclosure of Invention
The present invention aims to solve at least one of the above technical problems in the prior art. Therefore, the invention aims to provide a separation process of the four-carbon to six-carbon petroleum hydrocarbon, which is used for separating the four-carbon to six-carbon petroleum hydrocarbon sequentially through a prefractionator, a decarbonizing four-column, a five-carbon component separating column and an isohexane column, wherein the five-carbon component separating column is connected with the isohexane column in parallel, so that the separation energy consumption of the four-carbon to six-carbon petroleum hydrocarbon is greatly reduced, and the effective separation of the four-carbon to six-carbon petroleum hydrocarbon is ensured.
A second aspect of the present invention is to provide a separation device for carbon four to carbon six petroleum hydrocarbons.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows:
the first aspect of the invention provides a separation process of C four-to-C six-petroleum hydrocarbon, which is characterized in that the C four-to-C six-petroleum hydrocarbon is separated by a prefractionator, a decarbonization four-tower, a C five-component separation tower and an isohexane tower in sequence; the carbon five component separation tower is connected with the isohexane tower in parallel.
The invention changes the function of the first tower of the conventional four-tower sequential separation process of the decarbonization four-tower, the isopentane tower, the n-pentane tower and the isohexane tower from decarbonization four to prefractionation, which is called prefractionation, changes the second tower from isopentane tower to decarbonization four-tower, and changes the third tower from n-pentane tower to carbon five component separation tower, wherein the carbon five component separation tower and the isohexane tower are connected in parallel. The separation process greatly reduces the separation energy consumption of the four-carbon to six-carbon petroleum hydrocarbon and ensures the effective separation of the four-carbon to six-carbon petroleum hydrocarbon.
The four to six carbon petroleum hydrocarbons of the present invention include hydrocracked four to six carbon petroleum hydrocarbons and continuously reformed five to six carbon petroleum hydrocarbons.
In some embodiments of the invention, the prefractionation column overhead is carbon four to carbon five hydrocarbons and the bottoms is carbon five to carbon six hydrocarbons.
The corresponding tower top distillate of the prefractionator is changed from butane with the concentration of more than or equal to 99 percent by weight into C four-C five hydrocarbons (the mass content of C six hydrocarbons is controlled to be less than or equal to 0.01 per mill), and the C five-C six hydrocarbons are continuously distilled from the tower bottom.
In some embodiments of the invention, the decarbonized four column middle distillate is carbon five hydrocarbons, the overhead is carbon four hydrocarbons, and the bottoms is carbon six hydrocarbons.
In some embodiments of the invention, the carbon five component separation column overhead is isopentane and the bottoms is n-pentane.
In some embodiments of the invention, the isohexane column overhead is isohexane and the bottoms is n-hexane.
In some embodiments of the invention, the bottom of the prefractionator uses hot water as a source of reboiling heat.
In some embodiments of the invention, the bottom of the prefractionator takes hot water at 90-100 ℃ as a reboiling heat source.
In some embodiments of the invention, the bottom of the prefractionator takes hot water at 95-100 ℃ as a reboiling heat source.
In some examples of the invention, the prefractionator bottom uses 98 ℃ hot water as a source of reboiling heat.
According to the invention, after the first base tower is changed into the prefractionation tower, the operation pressure of the prefractionation tower is reduced, and meanwhile, the temperature of the bottom of the prefractionation tower is reduced due to the weakening of the separation strength, so that steam with the pressure of about 0.5MPa is not used as a reboiling heat source, and hot water is used as the reboiling heat source.
In some embodiments of the invention, the hot water is generated by recovering waste heat.
In some embodiments of the invention, the bottom reboiling reflux column temperature of the prefractionation column is 70-85 ℃.
In some embodiments of the invention, the bottom reboiling reflux column temperature of the prefractionation column is 75-85 ℃.
In some embodiments of the invention, the bottom reboiling reflux column temperature of the prefractionation column is 75-80 ℃.
Reboiling back to column temperature refers to the temperature at which the hydrocarbon component enters the column after passing through the bottom reboiler.
In some embodiments of the invention, the top temperature of the prefractionator is 40-50 ℃.
In some embodiments of the invention, the top temperature of the prefractionator is 40-45 ℃.
In some embodiments of the invention, the prefractionation column operates at a pressure of 50 to 120kPaG.
The operating pressures of the prefractionator, decarbonizing four column, carbon five component separator and isohexane column can be divided into the tadine pressure and the bottoms pressure.
In some embodiments of the invention, the prefractionation column operates at a pressure of 100 to 120kPaG.
In some embodiments of the invention, the top pressure of the prefractionator is between 90 and 110kPaG and the bottom pressure is between 110 and 130kPaG.
In some embodiments of the invention, the top pressure of the prefractionator is 95 to 105kPaG and the bottom pressure is 115 to 125kPaG.
In some embodiments of the invention, the prefractionator overhead is provided with an overhead gas compressor.
In some embodiments of the invention, the prefractionation column overhead gas is compressed to 200 to 600kPaG.
In some embodiments of the invention, the overhead gas compressor of the prefractionator compresses the overhead gas to 200 to 600kPaG.
The prefractionator is used for carrying out crude separation on raw materials, carbon four-carbon five hydrocarbons (the mass fraction of the carbon six hydrocarbons is below 0.01 per mill) are produced at the top of the prefractionator, the carbon five-carbon six hydrocarbons are produced at the bottom of the prefractionator, and a primary or secondary tower top gas compressor is arranged at the top of the prefractionator to compress tower top gas to 200-600 kPaG.
In some embodiments of the invention, the overhead gas compressor of the prefractionator compresses the overhead gas to 300 to 600kPaG.
In some examples of the invention, the overhead gas compressor of the prefractionator compresses the overhead gas to 200kPaG, 500kPaG, 600kPaG.
In some embodiments of the invention, the prefractionator is provided with a cooling system, the cooling system uses circulating cooling water as a refrigerant to control the operation temperature of a reflux tank in the reflux system to be 40-50 ℃, the top gas of the prefractionator is compressed by a top gas compressor, and the compressed gas is condensed and cooled and then enters the reflux tank.
In some embodiments of the invention, the cooling system of the prefractionator uses circulating cooling water as a coolant to control the operating temperature of the reflux drum in the reflux system to about 42 ℃.
In some embodiments of the invention, trays are provided in the decarbonizing four column, one side line is opened every 1-2 trays, and the carbon five hydrocarbons are extracted at the highest concentration.
The invention changes the function of the second column of the four-column sequential separation process from isopentane production to butane production, called decarbonization four-column, wherein the top of the column distillate feed decarbonization four-column from the prefractionation column, and the bottom of the column distillate feed decarbonization four-column from the prefractionation column.
In the decarbonizing four-column, the carbon five hydrocarbons are enriched in the middle part of the decarbonizing four-column, and for this purpose, one side line is opened every other or two column plates, and the total of three side lines is divided, and the carbon five hydrocarbons are extracted at the highest concentration. The butane product is produced at the top of the decarbonization four-column, and the carbon hexahydrocarbon is distilled at the bottom of the decarbonization four-column.
In some embodiments of the invention, the upper side feeding position of the decarburization four tower is positioned at 12 th to 17 th theoretical plate positions, the lower side feeding position is positioned at 85 th to 95 th theoretical plate positions, and the three side drawing outlets are positioned at 36 th to 44 th theoretical plate positions.
In some embodiments of the invention, the temperature of the side draw of the decarbonization four column is 80 to 90 ℃.
In some embodiments of the invention, the theoretical plate number of the decarburization four column is 120 to 130.
In some embodiments of the invention, steam is used as a reboiling heat source at the bottom of the decarburization four column.
In some embodiments of the invention, steam with the pressure of 0.45-0.55 MPa is used as a reboiling heat source at the bottom of the decarburization four-tower.
According to the invention, after the second tower is changed into the decarbonization four tower, compared with the isopentane tower in the conventional four-tower sequential separation process, the operation pressure of the decarbonization four tower is improved, so that the decarbonization four tower adopts 0.45-0.55 MPa steam as a reboiling heat source.
In some embodiments of the invention, 0.5MPa steam is used as a reboiling heat source at the bottom of the decarburization four-tower.
In some embodiments of the invention, the reboiling return column temperature of the decarbonization four column is 115 to 125 ℃.
In some embodiments of the invention, the reboiling return column temperature of the decarbonization four column is 118-125 ℃.
In some embodiments of the invention, the reboiling return column temperature of the decarbonization four column is 119-121 ℃.
In some embodiments of the invention, the top temperature of the decarbonization four-column is 40-60 ℃.
In some embodiments of the invention, the top temperature of the decarbonization four-column is 40-50 ℃.
In some embodiments of the invention, the temperature at the top of the decarbonization four-column is 45-50 ℃.
In some embodiments of the invention, the decarbonization four column is operated at a pressure of 400 to 500kPaG.
In some embodiments of the invention, the decarbonization four column is operated at a pressure of 400 to 450kPaG.
In some embodiments of the invention, the decarbonization four column is operated at a pressure of 400 to 420kPaG.
In some embodiments of the invention, the pressure at the top of the decarbonization four-column is 390 to 410kPaG, and the pressure at the bottom of the decarbonization four-column is 410 to 430kPaG.
In some embodiments of the invention, the pressure at the top of the decarbonization four-column is 395-405 kPaG, and the pressure at the bottom of the column is 415-425 kPaG.
In some embodiments of the invention, the bottom of the carbon five component separation column uses hot water as a reboiling heat source.
In some embodiments of the invention, the bottom of the carbon five component separation column uses hot water at 70-100 ℃ as a reboiling heat source.
The invention changes the function of the third tower of the four-tower sequential separation process from n-pentane production to the separation of carbon five, namely a carbon five component separation tower. The isopentane product is produced at the top of the carbon five component separation tower, and the n-pentane product is produced at the bottom of the carbon five component separation tower.
The system components of the carbon five component separation tower are lighter, and hot water with the temperature of 70-100 ℃ is used as a reboiling heat source at the bottom of the tower.
In some embodiments of the invention, the bottom reboiling reflux column temperature of the carbon five component separation column is from 55 to 65 ℃.
In some embodiments of the invention, the bottom reboiling reflux column temperature of the carbon five component separation column is 58 to 61 ℃.
In some embodiments of the invention, the bottom reboiling reflux column temperature of the carbon five component separation column is 59 to 60 ℃.
In some embodiments of the invention, the overhead temperature of the carbon five component separation column is 40 to 60 ℃.
In some embodiments of the invention, the overhead temperature of the carbon five component separation column is 40 to 50 ℃.
In some embodiments of the invention, the overhead temperature of the carbon five component separation column is 45 to 50 ℃.
In some embodiments of the invention, the operating pressure of the carbon five component separation column is 50 to 100kPaG.
In some embodiments of the invention, the operating pressure of the carbon five component separation column is from 80 to 100kPaG.
In some embodiments of the invention, the carbon five component separation column has a column top pressure of 70 to 90kPaG and a column bottom pressure of 90 to 110kPaG.
In some embodiments of the invention, the top pressure of the carbon five component separation column is 75 to 85kPaG and the bottom pressure is 95 to 105kPaG.
In some embodiments of the invention, the bottom of the isohexane column uses steam as a source of reboiling heat.
In some embodiments of the invention, 0.45-0.55 MPa steam is used as a reboiling heat source at the bottom of the isohexane tower.
The fourth column of the invention is also an isohexane column for separating the carbon hexahydrocarbons. The isohexane tower ejects out the isohexane and the normal hexane is obtained at the bottom of the isohexane tower.
In some embodiments of the invention, 0.5MPa steam is used as a reboiling heat source at the bottom of the isohexane tower.
In some embodiments of the invention, the bottom reboiling reflux column temperature of the isohexane column is from 85 to 95 ℃.
In some embodiments of the invention, the bottom reboiling reflux temperature of the isohexane column is from 88 to 92 ℃.
In some embodiments of the invention, the bottom reboiling reflux column temperature of the isohexane column is from 90 to 91 ℃.
In some embodiments of the invention, the overhead temperature of the isohexane column is from 40 to 60 ℃.
In some embodiments of the invention, the overhead temperature of the isohexane column is from 40 to 50 ℃.
In some embodiments of the invention, the overhead temperature of the isohexane column is from 45 to 50 ℃.
In the separation process, the third tower and the fourth tower are not connected in series any more and are connected in parallel, namely, the carbon five hydrocarbon and the carbon six hydrocarbon distilled from the decarburization four tower are treated respectively, so that the middle distillate back mixing is reduced.
In some embodiments of the invention, the isohexane column is operated at a pressure of from 100 to 200kPaG.
In some embodiments of the invention, the isohexane column is operated at a pressure of from 100 to 200kPaG.
In some embodiments of the invention, the isohexane column is operated at a pressure of from 100 to 120kPaG
In some embodiments of the invention, the isohexane column has a top pressure of from 90 to 110kPaG and a bottom pressure of from 110 to 130kPaG.
In some embodiments of the invention, the isohexane column has a top pressure of 95 to 105kPaG and a bottom pressure of 115 to 125kPaG.
In some embodiments of the invention, the prefractionator overhead gas acts as a reboiling heat source at the prefractionator bottom.
In some embodiments of the invention, the bottom reboiling heat source of the prefractionator further comprises prefractionator overhead gas waste heat.
The compressed top gas of the prefractionator has higher temperature and higher phase change thermal load, and the waste heat of the top gas can be used as a part of reboiling heat source at the bottom of the prefractionator by upgrading the heat pump flow. The flow arrangement is as follows: the compressed gas condensing cooler is arranged on the tower top platform, the machine pump is arranged to guide the liquid phase flow at the tower bottom to flow into the heat exchanger, after absorbing the phase change heat of the compressed gas, the liquid phase part (about 15 mol%) is gasified, and then the liquid phase part returns to the tower bottom with heat, so that the consumption of hot water is reduced, meanwhile, the cooling load at the tower top is reduced in an equivalent way, and the waste heat upgrading and utilization are realized.
In some embodiments of the invention, the reboiling heat source at the bottom of the carbon five component separation column comprises hot water after heat exchange with the reboiling heat source at the bottom of the prefractionator.
The bottoms of the prefractionator, the decarbonization four-tower, the carbon five-component separation tower and the isohexane tower are respectively provided with a reboiler, and reboiling heat sources are introduced into the reboilers.
In some embodiments of the present invention, the reboiling heat source hot water at the bottom of the carbon five component separation column is hot water after heat exchange by a reboiler at the bottom of the prefractionator, or the hot water after heat exchange is mixed with directly added hot water.
The bottom temperature of the carbon five component separation tower is lower, and hot water subjected to heat exchange by a reboiler at the bottom of the prefractionator can be used as a reboiling heat source at the bottom of the carbon five component separation tower.
In some embodiments of the invention, the reboiler of the prefractionator and the carbon five component separation column has a logarithmic heat transfer temperature difference of greater than or equal to 15 ℃.
The logarithmic heat transfer temperature refers to the logarithmic heat transfer temperature of each of the prefractionator and the carbon five component separation tower, and can be calculated by the following formula: Δtm= (Δt1- Δt2)/ln (Δt1/Δt2);
wherein, Δt1=t1-t2, Δt2=t2-t1, T1 is the initial temperature of the reboiling heat source hot water, T2 is the final temperature of the reboiling heat source hot water, T1 is the bottom temperature, and T2 is the reboiling return tower temperature.
In some embodiments of the invention, the carbon four to carbon six petroleum hydrocarbon comprises the following components: 8-12 wt% of butane, 25-40 wt% of isopentane, 13-20 wt% of n-pentane, 5-15 wt% of isohexane and 25-38 wt% of n-hexane.
In some embodiments of the invention, the carbon four to carbon six petroleum hydrocarbon comprises the following components: 8-10wt% of butane, 30-35wt% of isopentane, 15-17wt% of n-pentane, 9-1wt% of isohexane and 29-32wt% of n-hexane.
In some embodiments of the invention, the carbon four to carbon six petroleum hydrocarbon comprises the following components: 9-10wt% of butane, 30-33wt% of isopentane, 16-17wt% of n-pentane, 10-1wt% of isohexane and 31-32wt% of n-hexane.
In some embodiments of the invention, the prefractionation column has a reflux ratio of 4 to 5.
In some embodiments of the invention, the reflux ratio of the decarbonizing four towers is 20 to 26.
In some embodiments of the invention, the reflux ratio of the carbon five component separation column is 9 to 10.
In some embodiments of the invention, the isohexane column has a reflux ratio of from 8 to 9.
A second aspect of the present invention provides a separation apparatus for use in the carbon four to carbon six petroleum hydrocarbon separation process of the first aspect of the present invention, comprising a prefractionator, a decarbonizing four column, a carbon five component separator, an isohexane column;
the prefractionation tower is connected with the decarburization four towers; the decarbonization four towers are respectively connected with the carbon five component separation tower and the isohexane tower.
In some embodiments of the invention, the prefractionation column, decarbonizing four column, carbon five component separation column, isohexane column are all equipped with a reboiler, cooling system, reflux system.
In some embodiments of the invention, the cooling system comprises a chiller; the reflux system includes a reflux drum and a reflux pump.
In some embodiments of the invention, the prefractionation column, decarbonizing four column, carbon five component separation column, isohexane column are all equipped with a reboiler, cooler, reflux drum, reflux pump, and bottom pump.
In some embodiments of the invention, the prefractionator is provided with an overhead gas compressor.
Compared with the prior art, the invention has the beneficial effects that:
(1) The invention also provides a separation process of the carbon four-to-six-carbon petroleum hydrocarbon, which changes the conventional four-tower-isopentane tower-n-pentane tower-isohexane tower sequential separation into the separation sequentially passing through a prefractionator, a four-tower-decarbonizing tower, a five-carbon component separation tower and an isohexane tower, has strong flexibility, simultaneously connects the five-carbon component separation tower and the isohexane tower in parallel, reduces the energy consumption of the separation process, and can realize the effective separation of the carbon four-to-six-carbon petroleum hydrocarbon.
(2) According to the invention, reboiling heat sources of the prefractionator and the carbon five component separation tower are further changed into hot water generated by recovering low-temperature waste heat, so that the thermodynamic second law energy efficiency of the separation process of the carbon four-carbon six petroleum hydrocarbon is greatly improved, and the energy consumption cost is reduced.
(3) In the separation process, the compressed top gas of the prefractionator can be used as a reboiling heat source of the prefractionator and also can be used as a reboiling heat source of the carbon five-component separation tower, so that the energy consumption of the separation process is further reduced.
(4) The invention provides a separation device for four-to-six-carbon petroleum hydrocarbon, which changes a first tower in a four-tower sequential separation process from a decarburization four-tower to a prefractionation tower, changes a second tower from an isopentane tower to a decarburization four-tower, changes a third tower from a n-pentane tower to a five-carbon component separation tower, and simultaneously changes the original serial connection of the third tower and the fourth tower to parallel connection, thereby greatly reducing the energy consumption of the separation process for four-to-six-carbon petroleum hydrocarbon, reducing middle distillate back mixing and improving the rectification efficiency.
(5) The separation process and the separation device of the four-carbon to six-carbon petroleum hydrocarbon are suitable for new device construction and old device transformation.
Drawings
FIG. 1 is a schematic diagram showing a four-column separation apparatus and a flow chart of a decarbonization four-column isopentane column, n-pentane column and isohexane column of comparative example 1.
FIG. 2 is a flow chart showing a prefractionation column-decarbonization four column-carbon five component separation column-isohexane column sequential separation apparatus of example 1.
FIG. 3 is a flow chart showing a prefractionation column-decarbonization four column-carbon five component separation column-isohexane column sequential separation apparatus of example 2.
FIG. 4 is a flow chart showing a prefractionation column-decarbonization four column-carbon five component separation column-isohexane column sequential separation apparatus of example 3.
FIG. 5 is a flow chart showing a prefractionation column-decarbonization four column-carbon five component separation column-isohexane column sequential separation apparatus of example 4.
The numbering in fig. 1 is as follows:
1-decarbonization four towers; 2-decarbonization four-tower reboiler; 3-decarbonizing four-tower top gas circulating water cooler; 4-decarburization four-column top reflux tank; 5-decarbonizing four tower top product reflux pump; 6-decarburization four-column bottom pump; 7-isopentane column; 8-isopentane column reboiler; 9-isopentane tower top gas circulating water cooler; a 10-isopentane tower top reflux tank; a reflux pump for the 11-isopentane overhead product; a 12-isopentane tower bottom pump; 13-n-pentane tower; a 14-n-pentane column reboiler; 15-n-pentane tower top gas circulating water cooler; a 16-n-pentane tower top reflux tank; 17-n-pentane tower top product reflux pump; 18-n-pentane tower bottom pump; 19-isohexane column; 20-isohexane column reboiler; a 21-isohexane overhead gas circulating water cooler; a 22-isohexane overhead reflux drum; a reflux pump for the 23-isohexane overhead product; a bottom pump of the 24-isohexane tower.
The numbering in fig. 2 is as follows:
19-isohexane column; 20-isohexane column reboiler; a 21-isohexane overhead gas circulating water cooler; a 22-isohexane overhead reflux drum; a reflux pump for the 23-isohexane overhead product; a 24-isohexane tower bottom pump; 25-prefractionation column; 26-prefractionation column reboiler; 27-a prefractionation overhead gas compressor; 28-a prefractionation overhead gas circulating water cooler; 29-a prefractionation overhead reflux drum; 30-a reflux pump for prefractionation overhead product; 31-a prefractionator bottom pump; 32-decarbonizing four towers; 33-decarbonization four-tower reboiler; 34-decarbonizing four-tower top gas circulating water cooler; 35-decarbonizing a four-tower top reflux tank; 36-decarbonizing four tower top product reflux pump; 37-decarbonization four-tower bottom pump; 38-carbon five component separation tower; 39-a carbon five component separation column reboiler; a 40-carbon five component separation overhead gas recycle water cooler; a 41-carbon five component separation overhead reflux drum; a 42-carbon five component separation overhead reflux pump; a 43-carbon five component separation column top and bottom pump.
The descriptions of numbers 19-43 in FIGS. 3-5 are the same as FIG. 2, and the remaining numbers in FIGS. 3-5 are as follows:
44-reboiler.
Detailed Description
The present invention will be described in further detail with reference to specific examples. The starting materials, reagents or apparatus used in the examples and comparative examples were either commercially available from conventional sources or may be obtained by prior art methods unless specifically indicated. Unless otherwise indicated, assays or testing methods are routine in the art.
Comparative example 1
Comparative example 1 is a separation apparatus for carbon four to carbon six hydrocarbons having a certain treatment amount of 39.2 t/h. Wherein, C from hydrocracking unit 4 ～C 6 Hydrocarbon 35.1t/h, C from continuous reformer 5 ～C 6 Hydrocarbon 4.1t/h. The process of the comparative example aims at obtaining a product meeting the standard, and the quality standard of the product is as follows: butane with purity more than or equal to 99 percent, isopentane with purity more than or equal to 95 percent, n-pentane with purity more than or equal to 99 percent, isohexane with purity more than or equal to 99 percent and C with purity more than or equal to 99 percent 6 Hydrocarbons (n-hexane).
It should be noted that% wt and% wt represent mass fractions.
FIG. 1 is a schematic diagram showing a four-column separation apparatus and a flow chart of a decarbonization four-column isopentane column, n-pentane column and isohexane column of comparative example 1. In FIG. 1, the C four to C six hydrocarbons from the hydrocracking unit enter a decarbonizing four column 1, and are separated to obtain butane products from the top of the column and C from the bottom of the column 5 ～C 6 Hydrocarbons with C from a continuous reformer 5 ～C 6 Feeding hydrocarbon into isopentane column 7 together, separating to obtain isopentane product from top, feeding bottom fraction into n-pentane column 13, separating to obtain n-pentane product from top, and bottom C 6 The fraction is sent to an isohexane column 19, isohexane is obtained from the top of the column through separation, and n-hexane is obtained from the bottom. The bottom of the four towers uses 0.5MPa steam as a reboiling heat source, the top of the four towers uses circulating water as a cold source, and the temperature of the reflux tank is controlled to be about 40 ℃.
Table 1 shows the raw material composition of comparative example 1.
Table 1 comparative example 1 raw material composition
| No. | Component (A) | Unit (B) | Hydrocracking C 4 ～C 6 Hydrocarbons | Continuous reforming C 5 ～C 6 Hydrocarbons | Mixing raw materials |
| 1 | Butane | ％wt | 10.13 | 0.00 | 9.19 |
| 2 | Isopentane | ％wt | 31.44 | 38.38 | 32.14 |
| 3 | N-pentane | ％wt | 15.20 | 28.70 | 16.58 |
| 4 | Isohexane | ％wt | 11.55 | 1.56 | 10.46 |
| 5 | N-hexane | ％wt | 31.68 | 31.36 | 31.63 |
| Totalizing | ％wt | 100 | 100 | 100 | |
| Flow rate | t/h | 35.1 | 4.1 | 39.2 |
Table 2 shows the amounts and compositions of the products of comparative example 1.
Table 2 comparative example 1 product quantity and composition
| No. | Component (A) | Unit (B) | Butane | Isopentane | N-pentane | Isohexane | N-hexane |
| 1 | Butane | ％wt | 99.77 | 0.23 | 0.00 | 0.00 | 0.00 |
| 2 | Isopentane | ％wt | 0.23 | 95.77 | 0.32 | 0.00 | 0.00 |
| 3 | N-pentane | ％wt | 0.00 | 3.99 | 99.43 | 0.33 | 0.00 |
| 4 | Isohexane | ％wt | 0.00 | 0.01 | 0.25 | 99.67 | 0.20 |
| 5 | N-hexane | ％wt | 0.00 | 0.00 | 0.00 | 0.00 | 99.80 |
| Totalizing | ％wt | 100.00 | 100.00 | 100.00 | 100.00 | 100.00 | |
| Flow rate | t/h | 3.6 | 12.6 | 6.5 | 4.1 | 12.4 |
From the results in Table 2, it was demonstrated that each product was of acceptable quality.
Table 3 shows the main operating parameters of the four fractionation columns of comparative example 1.
Table 3 major operating parameters of comparative example 1 four fractionation columns
As can be seen from Table 3, the four-column total reboiling load is 2522.9X 10 4 kcal/h, 0.5MPag, 48.5t/h (150 ℃ for condensate temperature) for 190 ℃ superheated steam, 2246.7 multiplied by 10 for total overhead cooling load 4 kcal/h。
Example 1
Example 1 provides a separation device of four to six carbon petroleum hydrocarbon, and a separation process of four to six carbon petroleum hydrocarbon is provided based on the separation device, and the flow is shown in fig. 2.
FIG. 2 is a flow chart showing a prefractionation column-decarbonization four column-carbon five component separation column-isohexane column sequential separation apparatus of example 1.
In the figure, in the original technological process of comparative example 1, the rectification separation capability of the decarburization four towers is weakened, the cascade separation sequence is changed into the parallel separation sequence, and the specific process is as follows:
the mixed C four to C six hydrocarbons enter a prefractionation tower 25 for rectification separation, the operating pressure of the prefractionation tower 25 is reduced, and the tower is ejected C 4 ～C 5 Light hydrocarbon (C) 6 Less than 0.01 per mill by mass) is pressurized by a reflux pump 30 of a prefractionation tower top product and enters an upper feed inlet of a decarburization four tower 32; c at the bottom of the tower 5 ～C 6 The light hydrocarbon is pressurized by a decarbonization four-tower alkane bottom pump 31 and enters a lower feed inlet of an isopentane tower 32. The prefractionator 25 is provided with a first compressor 27 at the top of the column to convert low temperature and low pressureThe gas at the top of the tower is pressurized and heated, and then cooled to a reasonable temperature by an original cooling system. The prefractionation reboiler 26 uses 100 ℃ hot water as a reboiling heat source to heat and gasify part of the liquid in the tower bottom of the prefractionation tower 25 and return the liquid to the tower bottom.
Change C 4 ～C 6 The separation sequence of hydrocarbons. The decarbonization four tower 32 rectifies and separates the crude separation raw material from the prefractionation tower 25, the operating pressure of the decarbonization four tower 32 is increased, and butane products are produced at the top of the tower; intermediate C 5 Three side-line extraction ports are arranged at the light hydrocarbon enrichment part to extract C 5 Light hydrocarbon, C from bottom of tower 6 Light hydrocarbons.
C from the bottom of isopentane column 32 6 The light hydrocarbon keeps the original flow unchanged, and the qualified product is obtained by rectifying and separating by using the original isohexane tower 19. C from four-column side draw 5 The light hydrocarbons may also be separated using the n-pentane column 13 (i.e., the carbon five component separation column 38).
Wherein the logarithmic heat transfer temperature difference of the reboiler of the prefractionator and the reboiler of the carbon five component separation tower is more than or equal to 15 ℃. The logarithmic heat transfer temperature refers to the logarithmic heat transfer temperature of each of the prefractionator and the carbon five component separation tower, and can be calculated by the following formula: Δtm= (Δt1- Δt2)/ln (Δt1/Δt2);
Δt1=t1-T2, Δt2=t2-T1, T1 is the initial temperature of the reboiling heat source hot water, T2 is the final temperature of the reboiling heat source hot water, T1 is the bottom temperature, and T2 is the reboiling return column temperature.
In example 1, the prefractionation column T1 was 98℃and T2 was 90℃and the carbon five component separation column T1 was 98℃and T2 was 75 ℃.
The amount of raw materials, composition and product quality requirements in example 1 were the same as in comparative example 1.
Table 4 shows the amounts and compositions of the products of example 1.
TABLE 4 example 1 product quantity and composition
| No. | Component (A) | Unit (B) | Butane | Isopentane | N-pentane | Isohexane | N-hexane |
| 1 | Butane | ％wt | 99.88 | 0.07 | 0.00 | 0.00 | 0.00 |
| 2 | Isopentane | ％wt | 0.12 | 95.82 | 0.36 | 0.00 | 0.00 |
| 3 | N-pentane | ％wt | 0.00 | 4.10 | 99.43 | 0.34 | 0.00 |
| 4 | Isohexane | ％wt | 0.00 | 0.01 | 0.34 | 99.66 | 0.20 |
| 5 | N-hexane | ％wt | 0.00 | 0.00 | 0.00 | 0.00 | 99.80 |
| Totalizing | ％wt | 100.00 | 100.00 | 100.00 | 100.00 | 100.00 | |
| Flow rate | t/h | 3.6 | 12.6 | 6.5 | 4.1 | 12.4 |
It can be seen from table 4 that the product amounts and compositions are unchanged from the comparative examples, meeting the process requirements.
Table 5 shows the main operating parameters of the four fractionation columns of example 1.
Table 5 example 1 major operating parameters for four fractionation columns
It can be seen from table 5 that each column theory plate is unchanged. Example 1 Total reboiling and Total Cooling loads were 2703.4 ×10 respectively 4 kcal/h and 2669.7 ×10 4 kcal/h, total consumption of 0.5MPa steam 22.3t/h, total consumption of 98 ℃ hot water 1042.6t/h and power consumption of 641.8kw of the prefractionation overhead gas compressor. 220 yuan/t based on 0.5MPa steam and 0.93 yuan/10 hot water 4 Calculated as kcal, electricity 0.65 yuan/kWh and device year operation 8400 hours, example 1 reduced the cost of consumption 3245.5 ten thousand yuan/year compared to comparative example 1.
Example 2
Example 2 provides a separation device of four to six carbon petroleum hydrocarbon, and a separation process of four to six carbon petroleum hydrocarbon is provided based on the separation device, and the flow is shown in fig. 3.
On the basis of example 1, example 2 differs from the following:
1) The prefractionation column overhead gas compressor outlet pressure was raised from 200kPaG to 600kPaG of example 1, corresponding to 91.0 ℃;
2) Adding a reboiler 44 at the bottom of the prefractionator, and taking compressed gas as a reboiling heat source at the bottom of the prefractionator once;
the other procedure was unchanged from example 1.
Table 6 shows the product distribution and composition of example 2.
TABLE 6 product distribution and composition of example 2
| No. | Component (A) | Unit (B) | Butane | Isopentane | N-pentane | Isohexane | C 6 Component (A) |
| 1 | Butane | ％wt | 99.88 | 0.07 | 0.00 | 0.00 | 0.00 |
| 2 | Isopentane | ％wt | 0.12 | 95.82 | 0.36 | 0.00 | 0.00 |
| 3 | N-pentane | ％wt | 0.00 | 4.10 | 99.43 | 0.34 | 0.00 |
| 4 | Isohexane | ％wt | 0.00 | 0.01 | 0.34 | 99.66 | 0.20 |
| 5 | N-hexane | ％wt | 0.00 | 0.00 | 0.00 | 0.00 | 99.80 |
| Totalizing | ％wt | 100.00 | 100.00 | 100.00 | 100.00 | 100.00 | |
| Flow rate | t/h | 3.6 | 12.6 | 6.5 | 4.1 | 12.4 |
It can be seen from table 6 that the product amounts and compositions are unchanged from the comparative examples, meeting the process requirements.
Table 7 shows the main process parameters for the four columns of example 2.
TABLE 7 four column main process parameters of example 2
| No. | Project | Unit (B) | Prefractionation column | Decarbonization four towers | C 5 Separating tower | C 6 Separating tower |
| 1 | Overhead pressure | kPaG | 100 | 400 | 80 | 100 |
| 2 | Pressure of tower bottom | kPaG | 120 | 420 | 100 | 120 |
| 3 | Reflux ratio | Kg/Kg | 4.7 | 23.2 | 9.0 | 8.1 |
| 4 | Reflux amount | t/h | 66.1 | 83.5 | 113.9 | 33.3 |
| 5 | Overhead temperature | ℃ | 43.7 | 46.8 | 46.6 | 46.8 |
| 6 | Bottom temperature of column | ℃ | 75.8 | 120.6 | 59.4 | 90.4 |
| 7 | Reboiling the bottom of the tower and returning to the tower | ℃ | 76.5 | 120.9 | 59.4 | 90.4 |
| 8 | Cooling load | 10 4 kcal | 727.8 | 657.2 | 994.4 | 296.0 |
| 9 | Reboiling load | 10 4 kcal | 633.5 | 794.9 | 961.2 | 313.8 |
| 10 | Consume 0.5MPag steam | t/h | 0 | 15.6 | 0 | 6.7 |
| 11 | Consuming 98-90 deg.c hot water | t/h | 102.2 | 0 | 0 | 0 |
| 12 | Consuming 98-75 deg.c hot water | t/h | 0 | 0 | 361.4 | 0 |
| 13 | Compressor outlet pressure | kPaG | 600 | / | / | / |
| 14 | Compressor power consumption | kw | 1169.6 | / | / | / |
| 15 | Raw material feeding tower position | 31 | 15/90 | 46 | 71 | |
| 16 | Overhead product quantity | t/h | 14.0 | 3.6 | 12.6 | 4.1 |
| 17 | Bottom product quantity | t/h | 21.1 | 16.5 | 6.5 | 12.4 |
| 18 | Side draw amount | t/h | / | 19.1 | / | / |
| 19 | Side draw position | / | 38/40/42 | / | / | |
| 20 | Side draw temperature | ℃ | / | 88.0 | / | / |
| 21 | Number of theoretical plates | 70 | 120 | 92 | 129 |
As can be seen from Table 7, the total reboiling and total cooling loads of example 2 were 2703.4X 10, respectively 4 kcal/h and 2675.4 ×10 4 kcal/h, total consumption of 0.5MPa steam 22.3t/h, total consumption of 98 ℃ hot water 463.6t/h and power consumption of 1169.6kw of the prefractionation overhead gas compressor. 220 yuan/t based on 0.5MPa steam and 0.93 yuan/10 hot water 4 Calculated as kcal, electricity 0.65 yuan/kWh and device year operation 8400 hours, example 2 reduced energy consumption cost 3362.4 ten thousand yuan/year compared to comparative example 1.
Example 3
Example 3 provides a separation device for four to six carbon petroleum hydrocarbons, and a separation process for four to six carbon petroleum hydrocarbons is provided based on the separation device, and the flow is shown in fig. 4.
On the basis of example 1, example 3 differs from the following:
1) The prefractionation column overhead gas compressor outlet pressure was raised from 200kPaG to 500kPaG of example 1, corresponding to 84.3 ℃;
2) Increase C 5 The reboiler 44 at the bottom of the component separating tower uses compressed gas as C at one time 5 And reboiling the heat source at the bottom of the component separation tower.
The other procedure was unchanged from example 1.
Table 8 shows the product distribution and composition of example 3.
TABLE 8 product distribution and composition of example 3
| No. | Component (A) | Unit (B) | Butane | Isopentane | N-pentane | Isohexane | C 6 Component (A) |
| 1 | ≤C 4 | ％wt | 99.88 | 0.07 | 0.00 | 0.00 | 0.00 |
| 2 | Isopentane | ％wt | 0.12 | 95.82 | 0.36 | 0.00 | 0.00 |
| 3 | N-pentane | ％wt | 0.00 | 4.10 | 99.43 | 0.34 | 0.00 |
| 4 | Isohexane | ％wt | 0.00 | 0.01 | 0.34 | 99.66 | 0.20 |
| 5 | N-hexane | ％wt | 0.00 | 0.00 | 0.00 | 0.00 | 99.80 |
| Totalizing | ％wt | 100.00 | 100.00 | 100.00 | 100.00 | 100.00 | |
| Flow rate | t/h | 3.6 | 12.6 | 6.5 | 4.1 | 12.4 |
It can be seen from table 8 that the product amounts and compositions are unchanged from the comparative examples, meeting the process requirements.
Table 9 the four column main process parameters of example 3.
TABLE 9 four column main process parameters for example 3
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As can be seen from Table 9, the implementationExample 3 Total reboiling and Total Cooling loads were 2703.4 ×10 respectively 4 kcal/h and 2669.7 ×10 4 kcal/h, total consumption of 0.5MPa steam 22.3t/h, total consumption of 98 ℃ hot water 841.5t/h and power consumption of a prefractionation overhead gas compressor 1102.8kw. 220 yuan/t based on 0.5MPa steam and 0.93 yuan/10 hot water 4 Calculated as kcal, electricity 0.65 yuan/kWh and device year operation 8400 hours, example 3 reduced energy consumption cost 3411.6 ten thousand yuan/year compared to comparative example 1.
Example 4
Example 4 provides a separation device of four to six carbon petroleum hydrocarbons, and a separation process of four to six carbon petroleum hydrocarbons is provided based on the separation device, and the flow is shown in fig. 5.
Based on the embodiment 1, the reboiling heat source at the bottom of the carbon five component separation tower in the embodiment 4 is changed, and the method is as follows:
because the reboiling temperature of the bottom of the carbon five component separation tower is lower, C is increased 5 The reboiler 44 at the bottom of the component separation tower uses 98 ℃ hot water after heat exchange of the reboiler at the bottom of the prefractionation tower as a reboiling heat source at the bottom of the carbon five component separation tower. Thus, in example 4, the prefractionation column T1 was 98 ℃, T2 was 90 ℃, the carbon five component separation column T1 was 90 ℃, and T2 was 75 ℃.
The other procedure was unchanged from example 1.
Table 10 shows the product distribution and composition of example 4.
TABLE 10 product distribution and composition of example 4
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It can be seen from table 10 that the product amounts and compositions are unchanged from the comparative examples, meeting the process requirements.
Table 11 shows the main process parameters for the four columns of example 4.
TABLE 11 four column main process parameters for example 4
C in tables 5, 7, 9 and 11 5 Separation tower, C 6 The separation tower corresponds to a carbon five component separation tower and an isohexane tower respectively.
As can be seen from Table 11, the total reboiling and total cooling loads of example 4 were 2669.7X 10, respectively 4 kcal/h and 2727.4 ×10 4 kcal/h, total consumption of 0.5MPa steam 22.3t/h, total consumption of 98 ℃ hot water 681.2t/h and power consumption of 1102.8kw of the prefractionation overhead gas compressor. Example 4 saves 361.4t/h of hot water at 98℃as compared with example 1.
Comparative examples 1 to 4 and comparative example 1 show that the energy consumption of the conventional four-column sequential separation process of decarbonizing four-column, isopentane column, n-pentane column and isohexane column of comparative example 1 is greatly reduced, and the energy consumption cost is reduced to be not lower than 3200 ten thousand yuan/year by adopting the separation device of the four-to six-carbon petroleum hydrocarbon and the separation process of the four-to six-carbon petroleum hydrocarbon.
Compared with the embodiment 1, the embodiment 4 further adopts 98 ℃ hot water after heat exchange of a reboiler at the bottom of the prefractionator as a reboiling heat source at the bottom of the carbon five component separation tower, further reduces the energy consumption of the separation process, and saves 361.4t/h of the 98 ℃ hot water compared with the embodiment 1.
In summary, the four-carbon to six-carbon petroleum hydrocarbon separation device greatly reduces the energy consumption of the separation process of the four-carbon to six-carbon petroleum hydrocarbon, reduces the back mixing of middle distillates and improves the rectification efficiency. In the separation process, the conventional four-column sequential separation is changed into the separation by sequentially passing through the prefractionator, the decarbonization four-column, the carbon five-component separation column and the isohexane column, so that the separation process is high in flexibility and low in energy consumption, and meanwhile, the effective separation of the petroleum hydrocarbon with four to six carbon atoms can be realized, and the product quantity is not negatively influenced. In addition, the reboiling heat sources of the prefractionator and the carbon five component separation tower are further changed into hot water generated by residual heat of gas at the top of the prefractionator, so that the energy consumption cost can be further reduced.
The above examples are preferred embodiments of the present invention, but the embodiments of the present invention are not limited to the above examples, and any other changes, modifications, substitutions, combinations, and simplifications that do not depart from the spirit and principle of the present invention should be made in the equivalent manner, and the embodiments are included in the protection scope of the present invention.
Claims (10)
1. The separation process of the four-carbon to six-carbon petroleum hydrocarbon is characterized in that the four-carbon to six-carbon petroleum hydrocarbon is sequentially separated by a prefractionator, a decarbonization four-column, a five-carbon component separation column and an isohexane column; the carbon five component separation tower is connected with the isohexane tower in parallel.
2. The separation process of claim 1, wherein the prefractionator overhead is a carbon four to carbon five hydrocarbon and the bottoms is a carbon five to carbon six hydrocarbon;
and/or the middle fraction of the decarbonization four-tower is carbon five hydrocarbon, the top fraction is carbon four hydrocarbon, and the bottom fraction is carbon six hydrocarbon;
and/or the top fraction of the carbon five-component separation tower is isopentane, and the bottom fraction is n-pentane;
and/or the top fraction of the isohexane tower is isohexane, and the bottom fraction is n-hexane.
3. The separation process according to claim 1, wherein the bottom of the prefractionator uses hot water as a reboiling heat source;
and/or the temperature of the top of the prefractionator is 40-50 ℃;
and/or the operation pressure of the prefractionator is 50-120 kPaG;
and/or the top of the prefractionator is provided with a top gas compressor;
and/or compressing the top gas of the prefractionation column to 200-600 kPaG.
4. The separation process according to claim 1 or 2, wherein the bottom of the decarbonizing four-column takes steam as a reboiling heat source;
and/or the temperature of the top of the decarburization four-tower is 40-60 ℃;
and/or the operating pressure of the decarburization four column is 400 to 500kPaG.
5. The separation process according to claim 1, wherein the bottom of the carbon five component separation column uses hot water as a reboiling heat source;
and/or the temperature of the top of the carbon five-component separation tower is 40-60 ℃;
and/or the operating pressure of the carbon five component separation column is 50 to 100kPaG.
6. The separation process according to claim 1 or 2, wherein the bottom of the isohexane tower uses steam as a reboiling heat source;
and/or the temperature of the top of the isohexane tower is 40-60 ℃;
and/or the operating pressure of the isohexane tower is 100-200 kPaG.
7. The separation process of claim 3 or 5, wherein the prefractionator overhead gas is used as a reboiling heat source at the prefractionator bottom;
and/or the reboiling heat source at the bottom of the carbon five component separation tower comprises hot water after heat exchange with the reboiling heat source at the bottom of the prefractionator.
8. The separation process according to claim 1 or 2, wherein the difference in logarithmic heat transfer temperatures of the reboiler of the prefractionator and the carbon five component separation column is not less than 15 ℃.
9. The separation process according to claim 1 or 2, wherein the carbon four to carbon six petroleum hydrocarbon comprises the following components: 8-12 wt% of butane, 25-40 wt% of isopentane, 13-20 wt% of n-pentane, 5-15 wt% of isohexane and 25-38 wt% of n-hexane.
10. A separation device applied to the carbon four-to-carbon six-petroleum hydrocarbon separation process according to any one of claims 1 to 9, which is characterized by comprising a prefractionation column, a decarbonization four-column, a carbon five-component separation column and an isohexane column;
the prefractionation tower is connected with the decarburization four towers; the decarbonization four towers are respectively connected with the carbon five component separation tower and the isohexane tower.
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