CN115558521A - Optimized heavy naphtha processing technology - Google Patents
Optimized heavy naphtha processing technology Download PDFInfo
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- CN115558521A CN115558521A CN202211414997.6A CN202211414997A CN115558521A CN 115558521 A CN115558521 A CN 115558521A CN 202211414997 A CN202211414997 A CN 202211414997A CN 115558521 A CN115558521 A CN 115558521A
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- 238000012545 processing Methods 0.000 title claims abstract description 42
- 238000005516 engineering process Methods 0.000 title claims abstract description 13
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims abstract description 114
- 238000002407 reforming Methods 0.000 claims abstract description 71
- 239000001257 hydrogen Substances 0.000 claims abstract description 56
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 56
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 45
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 22
- 238000000034 method Methods 0.000 claims abstract description 22
- 238000006057 reforming reaction Methods 0.000 claims abstract description 17
- 238000001833 catalytic reforming Methods 0.000 claims abstract description 14
- 230000008569 process Effects 0.000 claims abstract description 14
- 239000003208 petroleum Substances 0.000 claims abstract description 13
- 239000002904 solvent Substances 0.000 claims description 61
- 239000007789 gas Substances 0.000 claims description 41
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 38
- 239000000463 material Substances 0.000 claims description 32
- 238000011084 recovery Methods 0.000 claims description 29
- 238000000895 extractive distillation Methods 0.000 claims description 27
- 238000000926 separation method Methods 0.000 claims description 23
- 239000000047 product Substances 0.000 claims description 21
- 238000006298 dechlorination reaction Methods 0.000 claims description 20
- 238000002156 mixing Methods 0.000 claims description 18
- 238000000605 extraction Methods 0.000 claims description 15
- 150000002431 hydrogen Chemical class 0.000 claims description 13
- 239000007791 liquid phase Substances 0.000 claims description 13
- 239000003054 catalyst Substances 0.000 claims description 12
- 239000007795 chemical reaction product Substances 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 11
- 238000005292 vacuum distillation Methods 0.000 claims description 11
- 238000005194 fractionation Methods 0.000 claims description 9
- 238000010521 absorption reaction Methods 0.000 claims description 8
- 238000006477 desulfuration reaction Methods 0.000 claims description 6
- 230000023556 desulfurization Effects 0.000 claims description 6
- 238000001179 sorption measurement Methods 0.000 claims description 6
- 230000009471 action Effects 0.000 claims description 5
- 238000003795 desorption Methods 0.000 claims description 5
- 239000002283 diesel fuel Substances 0.000 claims description 5
- 238000004821 distillation Methods 0.000 claims description 5
- 238000005086 pumping Methods 0.000 claims description 5
- 238000011049 filling Methods 0.000 claims description 2
- 238000010992 reflux Methods 0.000 claims description 2
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 claims description 2
- 230000035945 sensitivity Effects 0.000 claims 1
- 230000008901 benefit Effects 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 3
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 abstract description 3
- 125000003118 aryl group Chemical group 0.000 abstract 1
- 239000007788 liquid Substances 0.000 description 19
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 6
- 238000002474 experimental method Methods 0.000 description 6
- 239000000203 mixture Substances 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 4
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000000460 chlorine Substances 0.000 description 3
- 229910052801 chlorine Inorganic materials 0.000 description 3
- 238000011068 loading method Methods 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 238000013461 design Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
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- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G59/00—Treatment of naphtha by two or more reforming processes only or by at least one reforming process and at least one process which does not substantially change the boiling range of the naphtha
- C10G59/02—Treatment of naphtha by two or more reforming processes only or by at least one reforming process and at least one process which does not substantially change the boiling range of the naphtha plural serial stages only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/305—Octane number, e.g. motor octane number [MON], research octane number [RON]
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
Abstract
The invention discloses an optimized heavy naphtha processing technology, which is characterized in that original heavy naphtha is sent to a tank zone to be supplied to a naphtha hydrogenation unit of a catalytic reforming device to be optimized into a reforming unit of a direct catalytic reforming device for the heavy naphtha, and the heavy naphtha is purified and separated after reforming reaction to obtain high-octane gasoline, petroleum benzene, hydrogen and the like. Compared with the prior art, the method can improve the processing load of the reforming unit on the basis of unchanged processing load of the naphtha pre-hydrogenation unit, directly convert low value-added products (heavy naphtha) into high value-added products (high-octane gasoline, petroleum benzene and the like), and increase economic benefits; meanwhile, the process flow is short, the energy consumption is low, and the operation is convenient and simple; and the aromatic latent content of the heavy naphtha is 60-65%, the feeding quality of a reforming unit is improved, and the octane number of the product reformed gasoline is improved.
Description
Technical Field
The invention relates to the field of oil refining, in particular to an optimized heavy naphtha processing technology.
Background
The conventional oil refining system generally comprises an atmospheric and vacuum distillation unit, a catalytic cracking unit, a delayed coking unit, a catalytic reforming unit, a hydrorefining unit, a hydro-upgrading unit and the like, wherein the catalytic reforming unit is an important oil refining process which takes naphtha as a raw material to produce high-octane gasoline and light aromatic hydrocarbons and simultaneously produces hydrogen as a byproduct. Heavy naphtha is a product of a hydrogenation modification device in a refinery, the distillation range of the heavy naphtha is 102-175 ℃, the contents of sulfur, nitrogen and chlorine are below 5ppm, and the content of aromatic hydrocarbon is 60-65%. The design yield of the refined naphtha produced by the pre-hydrogenation unit of the catalytic reforming device is 88.88 percent, but in the actual production operation process, the yield of the refined naphtha is only about 82 percent because of more light components of the processed naphtha. Taking a certain device as an example, the processing scale of a reforming unit of a catalytic reforming device is 40 ten thousand tons/year, the processing scale of a pre-hydrogenation unit is 45 ten thousand tons/year, the total feeding amount of the pre-hydrogenation unit is 54t/h according to 100 percent of design load, and the refined naphtha entering the reforming unit after light components such as topping oil are separated and removed is 47.6t/h; in the actual production process, the total feeding amount of the pre-hydrogenation unit is 54t/h, the refined naphtha amount entering the reforming unit is 44.2t/h after light components such as topped oil are separated and removed, the load cannot reach 100%, and the yield of high-octane gasoline, light aromatic hydrocarbon and hydrogen is severely restricted; meanwhile, heavy naphtha gets away with the process flow of desulfurization, denitrification, dechlorination, stripping and fractionation of a pre-hydrogenation unit once again, so that the energy consumption is increased, the difficulty of the operation process is increased, and the potential safety hazard is increased.
Disclosure of Invention
The technical problem to be solved by the invention is to provide an optimized heavy naphtha processing technology, the heavy naphtha is directly supplied to a reforming unit for reforming reaction by changing the processing path of the heavy naphtha, the technological process is short, the energy consumption is low, the operation is convenient and simple, and low value-added products are directly converted into high value-added products; on the basis of changing the processing load of the pre-hydrogenation unit by 100%, the processing load of the reforming unit is increased from 90% to 100%, so that the loads of all devices of the whole system are more matched; the quality of the feed to the reforming unit is improved, thereby increasing the octane number of the reformed gasoline.
In order to solve the technical problems, the invention comprises a four-in-one heating furnace, four corresponding reforming reactors, a reforming recycle hydrogen compressor, a reformate knockout drum, a reforming hydrogen supercharger, a contact tank, a hydrogen dechlorination tank, a liquefied gas absorption tank, a PSA unit, a depentanizer, a de-C6 tower, a C4/C5 knockout drum, an extraction feed buffer tank, an extraction distillation tower, a solvent recovery tower and a benzene tower; reflux tanks are arranged at the tops of the depentanizer, the C6-removing tower, the C4/C5 separation tower, the extractive distillation tower, the solvent recovery tower and the benzene tower, and the method comprises the following steps:
mixing heavy naphtha from a diesel oil upgrading device with refined naphtha obtained by desulfurization, denitrification, dechlorination, stripping and fractionation of a pre-hydrogenation unit of a catalytic reforming device, mixing the heavy naphtha with hydrogen, sequentially feeding the mixture into a four-in-one heating furnace and four corresponding reforming reactors to react under the action of a reforming catalyst, and feeding the mixture into a reforming product separating tank to separate to obtain hydrogen and a reforming reaction product;
the step (2) is contacted again, the reforming reaction product in the step (1) is sent into a re-contact tank, the pressure is increased by a reforming hydrogen booster, the purity of reforming hydrogen and the product liquid yield can be improved, and liquid phase materials enter a depentanizer after liquefied gas is separated by a liquefied gas absorption tank;
the reformed hydrogen at the top of the re-contact tank enters a PSA unit after dechlorination through a hydrogen dechlorination tank, and high-purity hydrogen and desorbed gas are obtained through multiple times of adsorption and desorption of the PSA unit and are sent out of the device;
fractionating the reforming product in the step (3), fractionating materials in a depentanizer, sending C4/C5 components generated at the tower top to a C4/C5 separation tower, and sending more than C6 components at the tower bottom to a C6 removal tower;
fractionating materials in the C6-removing tower, sending C6 generated at the top of the tower to a benzene extraction unit, and sending high-octane gasoline at the bottom of the tower out of the device;
fractionating materials in the C4/C5 separation tower, sending liquefied gas generated at the tower top out of the device, and sending pentane oil at the tower bottom out of the device;
step (4), carrying out extractive distillation, wherein C6 from the C6 removing tower and a poor solvent from the solvent recovery tower enter an extractive distillation tower for extractive distillation, raffinate oil generated at the top of the extractive distillation tower is sent out of a device, and a rich solvent at the bottom of the tower enters a solvent recovery tower;
and (5) recovering the solvent, wherein the rich solvent entering the solvent recovery tower is subjected to vacuum distillation, crude benzene generated at the top of the tower enters a benzene tower, high-purity petroleum benzene is obtained by pumping out from the lateral line of the benzene tower, and the poor solvent at the bottom of the tower is recycled in the system.
The operating temperature of the four reforming reactor inlets in the step (1) is 475-500 ℃; in the four reforming reactors, the filling ratio of the catalyst in the first reforming reactor to the catalyst in the fourth reforming reactor is 1 (1.4-1.6): (2.4-2.6): 4.9-5.1).
The operating temperature of the depentanizer in the step (3) is 200-220 ℃, and the operating pressure is 0.95-1.05MPa;
the operating temperature of the C6 removing tower is 140-160 ℃, and the operating pressure is 0.04-0.06MPa;
the operating temperature of the C4/C5 separation tower is 124-140 ℃, and the operating pressure is 1.15-1.35MPa.
The lean solvent in the step (4) is sulfolane, the mass ratio of the lean solvent to the C6 is 2.5-5:1, and the operating temperature of a sensitive plate of the extractive distillation tower is 120 +/-10 ℃.
And (5) the vacuum distillation pressure of the solvent recovery tower is-0.034 +/-0.01 MPa.
Compared with the prior art, the invention has the following beneficial effects: the heavy naphtha is directly supplied to the reforming unit through transformation, processing equipment of the pre-hydrogenation unit, such as a pre-hydrogenation heating furnace, a pre-hydrogenation reactor, a pre-hydrogenation dechlorination reactor, a stripping tower, a fractionating tower and the like, is spanned, the processing load of the pre-hydrogenation unit is reduced, the processing load of the reforming unit is improved, the upstream and downstream operation loads are more matched, the hydrogen and high value-added product yield is effectively increased, and the economic benefit is increased.
(1) The invention changes the processing path of heavy naphtha, the heavy naphtha does not pass through the pre-hydrogenation unit any more, the process flow is short, the processing load of the reforming unit is increased (the processing load is increased from 90 percent to 100 percent), and the hydrogen production is increased by 800Nm 3 The output is improved by 7 percent, and the hydrogen balance of the whole plant is optimized;
(2) According to the invention, the heavy naphtha is utilized to the maximum extent, the heavy naphtha directly enters the reforming unit to react, and low value-added products (the heavy naphtha) are directly converted into high value-added products (high-octane gasoline, petroleum benzene and the like), so that the economic benefit is increased;
(3) The method optimizes the feeding property of the reforming unit, adjusts the feeding of refined naphtha (with 50% of aromatic hydrocarbon content) into the mixed feeding of the refined naphtha and the heavy naphtha, and improves the feeding quality of the reforming unit so as to improve the octane number of the product reformed gasoline, wherein the aromatic hydrocarbon content of the heavy naphtha is 60-65%.
Drawings
FIG. 1 is a schematic process flow diagram of the present invention;
FIG. 2 is a schematic flow diagram of a conventional heavy naphtha processing process.
Detailed Description
In order to more clearly understand the technical features, objects, and effects of the present invention, specific embodiments of the present invention will now be described.
Referring to fig. 1, the optimized heavy naphtha processing technology of the invention comprises a pre-hydrogenation unit fractionating tower, wherein the fractionating tower is provided with a light naphtha gas outlet and a refined naphtha liquid outlet, and the gas outlet is connected to a C4/C5 separating tower through a pipeline; the refined naphtha liquid and the heavy naphtha liquid of the hydrogenation upgrading device are mixed and then are connected to a four-in-one heating furnace, four reforming reactors and a reformate knockout drum which correspond to the four heating furnace through pipelines; the reformed product separation tank is provided with a reformed reaction product material inlet, a reformed hydrogen gas outlet and a liquid phase material outlet, the gas outlet is respectively connected to the reformed circulating hydrogen compressor, the reformed hydrogen supercharger and the re-contact tank through pipelines, and the liquid phase material outlet is connected to the re-contact tank through a pipeline; the contact tank is provided with a material inlet, a reformed hydrogen gas outlet and a liquid-phase material outlet, and the gas outlet is connected to a hydrogen dechlorination tank and a PSA (pressure swing adsorption) unit through pipelines in sequence; the liquid phase material outlet is connected to a liquefied gas absorption tank and a depentanizer sequentially through pipelines; the depentanizer is provided with a liquid phase material inlet, a C4/C5 component gas outlet and a component liquid outlet with the component number of more than 6, and the gas outlet is connected to the C4/C5 separation tower through a pipeline; the liquid outlet is connected to the de-C6 tower through a pipeline; the C4/C5 separation tower is provided with a material inlet, a liquefied gas outlet and a pentane liquid outlet, and the liquefied gas is sent out of the device through the gas outlet; the liquid outlet sends out pentane oil from the device; the C6-removing tower is provided with a material inlet, a C6 component gas outlet and a high-octane gasoline liquid outlet, the gas outlet is connected to the extraction feeding buffer tank and the extraction distillation tower through pipelines in sequence, and the high-octane gasoline is sent out of the device through the liquid outlet; the extraction distillation tower is provided with two material inlets, a raffinate oil gas outlet and a rich solvent liquid outlet, wherein the two material inlets are respectively a lean solvent inlet and a C6 inlet, the raffinate oil is sent out of the device by the gas outlet, and the liquid outlet is connected to the solvent recovery tower through a pipeline; the solvent recovery tower is provided with a material inlet, a crude benzene gas outlet and a lean solvent liquid outlet, and the gas outlet is connected to the benzene tower through a pipeline; the liquid outlet is connected to the extractive distillation column through a pipeline; the benzene tower is provided with a crude benzene material inlet and a petroleum benzene liquid outlet, and the petroleum benzene is sent out of the device through the liquid outlet.
The equipment is universal equipment for refineries, all the equipment are connected by pipelines according to the process requirements, and necessary sensors such as pumps, valves, temperature, pressure, flow and the like are arranged.
Example 1
The optimized heavy naphtha processing technology adopts the equipment, and the heavy naphtha processing comprises reforming reaction, recontacting, reformate fractionation, extractive distillation and solvent recovery. In this embodiment, the processing scale of the catalytic reforming unit is 40 ten thousand tons/year, and the method specifically includes the following steps:
mixing heavy naphtha from a diesel oil upgrading device with refined naphtha obtained by desulfurization, denitrification, dechlorination, stripping and fractionation of a pre-hydrogenation unit of a catalytic reforming device, mixing the mixed naphtha with hydrogen, feeding the mixed naphtha with the hydrogen into a four-in-one heating furnace and four corresponding reforming reactors, and carrying out various reactions under the action of reforming catalysts to obtain reforming reaction products.
The flow rate in the reforming reactor was 46t/h.
The operating temperature of the reforming reactor inlet was 475 ℃.
The catalyst loading ratio of the reforming reactors, the first reforming reactor to the fourth reforming reactor is 1.
Feeding the reforming reaction product from the reforming product separation tank into a re-contact tank, increasing the pressure by a reforming hydrogen booster, separating liquid-phase material from liquefied gas by a liquefied gas absorption tank, and feeding the liquid-phase material into a depentanizer;
and the reformed hydrogen at the top of the re-contact tank enters the PSA unit after dechlorination in the hydrogen dechlorination tank, and high-purity hydrogen and desorbed gas are obtained after multiple times of adsorption and desorption in the PSA unit.
The pressure of the recontacting tank is increased by a reformed hydrogen booster so as to improve the purity of the reformed hydrogen and the yield of the product liquid.
Fractionating the depentanizer in the step (3), sending light components generated at the top of the depentanizer to a C4/C5 separation tower, and sending materials at the bottom of the depentanizer to a C6 removal tower;
the operating temperature of the depentanizer is 200 ℃ and the operating pressure is 0.95MPa.
Fractionating the C6 removing tower, sending C6 generated at the tower top to an extraction feeding buffer tank, and obtaining high-octane gasoline at the tower bottom;
the operating temperature of the C6 removing tower is 140 ℃, and the operating pressure is 0.04MPa.
The feeding amount of the C6 to the extraction feeding buffer tank is 11583kg/h, and the yield of the high-octane gasoline is 30375kg/h.
Fractionating the C4/C5 separation tower to obtain liquefied gas at the tower top and pentane oil at the tower bottom;
the operating temperature of the C4/C5 separation tower is 124 ℃, and the operating pressure is 1.15MPa.
The yield of the liquefied gas is 958kg/h, and the yield of pentane oil is 9250kg/h.
And (4) feeding the C6 from the C6 removing tower and the lean solvent from the solvent recovery tower into an extractive distillation tower for extractive distillation, sending raffinate oil generated at the top of the extractive distillation tower out of the device, and feeding the rich solvent at the bottom of the tower into the solvent recovery tower.
The mass ratio of the lean solvent to C6 is 2.5.
The raffinate oil yield was 8875kg/h.
And (5) the rich solvent entering the solvent recovery tower is subjected to vacuum distillation, crude benzene generated at the tower top enters a benzene tower, high-purity petroleum benzene is obtained by pumping out from the side line of the benzene tower, and the poor solvent at the tower bottom is recycled in the system.
The vacuum distillation pressure of the solvent recovery tower is-0.024 MPa.
The petroleum benzene yield is 2208kg/h.
By utilizing the heavy naphtha processing technology optimized in the embodiment, the initial boiling point of a material (a mixture of refined naphtha and heavy naphtha) entering the reforming reaction can be increased from 78 ℃ to 80 ℃, the processing amount is increased from 44.2t/h to 46t/h, and the hydrogen production is increased to 340Nm 3 H; the output of the pentane oil product is reduced from 260 tons/day to 220 tons/day, the quality of the pentane oil is improved, and the content of C4 in the pentane oil is reduced from 15 percent to 5 percent; meanwhile, the yield of the gasoline component reformed gasoline is improved from 700 tons/day to 730 tons/day, and the yield is improved by 4.3 percent.
Example 2
The optimized heavy naphtha processing technology adopts the equipment, and the heavy naphtha processing comprises reforming reaction, recontacting, reformate fractionation, extractive distillation and solvent recovery. In this embodiment, the processing scale of the catalytic reforming unit is 40 ten thousand tons/year, and the method specifically includes the following steps:
mixing heavy naphtha from a diesel oil upgrading device with refined naphtha obtained by desulfurization, denitrification, dechlorination, stripping and fractionation of a pre-hydrogenation unit of a catalytic reforming device, mixing the mixed naphtha with hydrogen, feeding the mixed naphtha with the hydrogen into a four-in-one heating furnace and four corresponding reforming reactors, and carrying out various reactions under the action of reforming catalysts to obtain reforming reaction products.
The flow rate in the reforming reactor was 48.2t/h.
The operating temperature of the reforming reactor inlet was 500 ℃.
The catalyst loading ratio of the first reforming reactor to the fourth reforming reactor is 1.6.
Feeding the reforming reaction product from the reforming product separation tank into a re-contact tank, increasing the pressure by a reforming hydrogen booster, separating liquid-phase material from liquefied gas by a liquefied gas absorption tank, and feeding the liquid-phase material into a depentanizer;
and the reformed hydrogen at the top of the re-contact tank enters the PSA unit after dechlorination in the hydrogen dechlorination tank, and high-purity hydrogen and desorbed gas are obtained after multiple times of adsorption and desorption in the PSA unit.
The pressure of the re-contact tank is increased by a reformed hydrogen booster so as to improve the purity of the reformed hydrogen and the yield of the product liquid.
Fractionating the depentanizer in the step (3), sending light components generated at the top of the depentanizer to a C4/C5 separation tower, and sending materials at the bottom of the depentanizer to a C6 removal tower;
the operating temperature of the depentanizer is 220 ℃ and the operating pressure is 1.05MPa.
Fractionating the C6 removing tower, sending C6 generated at the tower top to an extraction feeding buffer tank, and obtaining high-octane gasoline at the tower bottom;
the operating temperature of the de-C6 tower is 160 ℃, and the operating pressure is 0.06MPa.
The feeding amount of the C6 to the extraction feeding buffer tank is 12333kg/h, and the output of the high-octane gasoline is 33458kg/h.
Fractionating the C4/C5 separation tower to obtain liquefied gas at the tower top and pentane oil at the tower bottom;
the operating temperature of the C4/C5 separation tower is 140 ℃, and the operating pressure is 1.35MPa.
The yield of the liquefied gas is 1041kg/h, and the yield of pentane oil is 10000kg/h.
And (4) feeding the C6 from the C6 removing tower and the lean solvent from the solvent recovery tower into an extractive distillation tower for extractive distillation, sending raffinate oil generated at the top of the extractive distillation tower out of the device, and feeding the rich solvent at the bottom of the tower into the solvent recovery tower.
The mass ratio of the lean solvent to the C6 is 5:1, and the operating temperature of a sensitive plate of the extractive distillation tower is 130 ℃.
The raffinate oil yield was 10083kg/h.
And (5) the rich solvent entering the solvent recovery tower is subjected to vacuum distillation, crude benzene generated at the tower top enters a benzene tower, high-purity petroleum benzene is obtained by pumping out from the side line of the benzene tower, and the poor solvent at the tower bottom is recycled in the system.
The vacuum distillation pressure of the solvent recovery tower is-0.044 MPa.
The petroleum benzene yield is 2708kg/h.
By utilizing the heavy naphtha processing technology optimized in the embodiment, the initial boiling point of a material (a mixture of refined naphtha and heavy naphtha) entering the reforming reaction can be increased from 78 ℃ to 85 ℃, the processing amount is increased from 44.2t/h to 48.2t/h, and 800Nm (Nm) of hydrogen is produced more 3 H; the output of the pentane oil product is reduced from 280 tons/day to 240 tons/day, the quality of the pentane oil is improved, and the content of C4 in the pentane oil is reduced from 15 percent to 5 percent; meanwhile, the yield of the gasoline component reformed gasoline is improved from 700 tons/day to 800 tons/day, and the yield is improved by 14 percent.
Example 3
The optimized heavy naphtha processing technology adopts the equipment, and the heavy naphtha processing comprises reforming reaction, recontacting, reformate fractionation, extractive distillation and solvent recovery. In this embodiment, the processing scale of the catalytic reforming unit is 40 ten thousand tons/year, and the method specifically includes the following steps:
mixing heavy naphtha from a diesel oil upgrading device with refined naphtha obtained by desulfurization, denitrification, dechlorination, stripping and fractionation of a pre-hydrogenation unit of a catalytic reforming device, mixing the mixed naphtha with hydrogen, feeding the mixed naphtha with the hydrogen into a four-in-one heating furnace and four corresponding reforming reactors, and carrying out various reactions under the action of reforming catalysts to obtain reforming reaction products.
The flow rate in the reforming reactor was 47.5t/h.
The operating temperature of the reforming reactor inlet was 485 ℃.
The catalyst loading ratio of the first reforming reactor to the fourth reforming reactor is 1.5.
Feeding the reforming reaction product from the reforming product separation tank into a re-contact tank, increasing the pressure by a reforming hydrogen booster, separating liquid-phase material from liquefied gas by a liquefied gas absorption tank, and feeding the liquid-phase material into a depentanizer;
and the reformed hydrogen at the top of the re-contact tank enters the PSA unit after dechlorination in the hydrogen dechlorination tank, and high-purity hydrogen and desorbed gas are obtained after multiple times of adsorption and desorption in the PSA unit.
The pressure of the re-contact tank is increased by a reformed hydrogen booster so as to improve the purity of the reformed hydrogen and the yield of the product liquid.
Fractionating the depentanizer in the step (3), sending light components generated at the top of the depentanizer to a C4/C5 separation tower, and sending materials at the bottom of the depentanizer to a C6 removal tower;
the operating temperature of the depentanizer is 210 ℃ and the operating pressure is 1.0MPa.
Fractionating the C6 removing tower, sending C6 generated at the tower top to an extraction feeding buffer tank, and obtaining high-octane gasoline at the tower bottom;
the operating temperature of the de-C6 tower is 150 ℃, and the operating pressure is 0.05MPa.
The feeding amount of the C6 to the extraction feeding buffer tank is 12014kg/h, and the output of the high-octane gasoline is 32025kg/h.
Fractionating the C4/C5 separation tower to obtain liquefied gas at the tower top and pentane oil at the tower bottom;
the operating temperature of the C4/C5 separation tower is 132 ℃, and the operating pressure is 1.25MPa.
The yield of the liquefied gas is 1004kg/h, and the yield of pentane oil is 97630kg/h.
And (4) feeding the C6 from the C6 removing tower and the lean solvent from the solvent recovery tower into an extractive distillation tower for extractive distillation, sending raffinate oil generated at the top of the extractive distillation tower out of the device, and feeding the rich solvent at the bottom of the tower into the solvent recovery tower.
The mass ratio of the lean solvent to the C6 is 4:1, and the operating temperature of a sensitive plate of the extractive distillation tower is 120 ℃.
The raffinate oil yield was 9368kg/h.
And (5) the rich solvent entering the solvent recovery tower is subjected to vacuum distillation, crude benzene generated at the tower top enters a benzene tower, high-purity petroleum benzene is obtained by pumping out from the side line of the benzene tower, and the poor solvent at the tower bottom is recycled in the system.
The vacuum distillation pressure of the solvent recovery tower is-0.034 MPa.
The petroleum benzene yield is 2585kg/h.
By utilizing the heavy naphtha processing technology optimized in the embodiment, the initial boiling point of the feed (the mixture of refined naphtha and heavy naphtha) of the reforming unit can be increased from 78 ℃ to 82 ℃, the processing amount can be increased from 44.2t/h to 47t/h, and 600Nm (Nm) of hydrogen can be produced 3 H; the output of the pentane oil product is reduced from 280 tons/day to 255 tons/day, the quality of the pentane oil is improved, and the content of C4 in the pentane oil is reduced from 15 percent to 5 percent; meanwhile, the yield of the gasoline component reformed gasoline is improved from 700 tons/day to 760 tons/day, and the yield is improved by 8.5 percent.
Comparative example
The optimized heavy naphtha processing process of example 1 was used to give experimental results for different ratios of the feed properties of the reforming unit after blending heavy naphtha in step (1).
The properties of the reforming unit feed (refined naphtha) without heavy naphtha are shown in the following table:
after mixing the heavy naphtha and the refined naphtha according to the procedure (1) of example 1, three experiments were carried out, respectively, in which the amount of the heavy naphtha blended in each experiment was as follows:
experiment 1: the blending flow rate of heavy naphtha is 1502kg/h, and the blending proportion is 3.1%.
Experiment 2: the blending flow rate of the heavy naphtha is 2013kg/h, and the blending proportion is 4.1%.
Experiment 3: the blending flow rate of the heavy naphtha is 2516kg/h, and the blending proportion is 5.2%.
The contents of sulfur, nitrogen, chlorine, water and metals in the refined naphtha in the experiments 1 to 3 were detected as follows:
from the above table, it can be seen that after heavy naphtha is blended, the contents of sulfur, nitrogen and chlorine in the feed of the reforming unit can be controlled to be below 0.5ppm, which meets the requirements of raw materials for processing of the reforming unit, and the content of aromatic hydrocarbon is increased, thereby improving the quality of the feed of the reforming unit.
All percentages used in the present invention are mass percentages unless otherwise indicated.
Finally, it should be noted that: although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that changes may be made in the embodiments and/or equivalents thereof without departing from the spirit and scope of the invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (5)
1. An optimized heavy naphtha processing technology comprises a four-in-one heating furnace, four reforming reactors corresponding to the four heating furnace, a reforming recycle hydrogen compressor, a reformate knockout drum, a reforming hydrogen supercharger, a re-contact tank, a hydrogen dechlorination tank, a liquefied gas absorption tank, a PSA unit, a depentanizing tower, a C6-removing tower, a C4/C5 knockout drum, an extraction feeding buffer tank, an extraction distillation tower, a solvent recovery tower and a benzene tower; the top of the depentanizer, the C6-removing tower, the C4/C5 separation tower, the extractive distillation tower, the solvent recovery tower and the benzene tower is provided with a reflux tank, and the method is characterized by comprising the following steps:
mixing heavy naphtha from a diesel oil modifying device with refined naphtha obtained by desulfurization, denitrification, dechlorination, stripping and fractionation of a pre-hydrogenation unit of a catalytic reforming device, mixing the mixed naphtha with hydrogen, sequentially feeding the mixed naphtha with the hydrogen into a four-in-one heating furnace and four corresponding reforming reactors, reacting under the action of a reforming catalyst, and feeding the mixed naphtha into a reforming product separating tank for separation to obtain hydrogen and a reforming reaction product;
the second contact of the step (2), the reforming reaction product of the step (1) is sent into a second contact tank, the pressure is increased by a reforming hydrogen booster, and the liquefied gas is separated from the liquid phase material by a liquefied gas absorption tank and then enters a depentanizer;
the reformed hydrogen at the top of the re-contact tank enters a PSA unit after dechlorination through a hydrogen dechlorination tank, and high-purity hydrogen and desorbed gas are obtained through multiple times of adsorption and desorption of the PSA unit and are sent out of the device;
fractionating the reformate in the step (3), fractionating materials in a depentanizer, sending C4/C5 components generated at the tower top to a C4/C5 separation tower, and sending more than C6 components at the tower bottom to a C6 removal tower;
fractionating materials in the C6-removing tower, sending C6 generated at the top of the tower to a benzene extraction unit, and sending high-octane gasoline at the bottom of the tower to a device;
fractionating materials in the C4/C5 separation tower, sending liquefied gas generated at the tower top out of the device, and sending pentane oil at the tower bottom out of the device;
step (4), carrying out extractive distillation, wherein C6 from the C6 removing tower and a poor solvent from the solvent recovery tower enter an extractive distillation tower for extractive distillation, raffinate oil generated at the top of the extractive distillation tower is sent out of a device, and a rich solvent at the bottom of the tower enters a solvent recovery tower;
and (5) recovering the solvent, wherein the rich solvent entering the solvent recovery tower is subjected to vacuum distillation, crude benzene generated at the top of the tower enters a benzene tower, high-purity petroleum benzene is obtained by pumping out from the lateral line of the benzene tower, and the poor solvent at the bottom of the tower is recycled in the system.
2. The optimized heavy naphtha processing process of claim 1, wherein the operating temperature of the four reforming reactor inlets of step (1) is 475-500 ℃; in the four reforming reactors, the filling ratio of the catalyst in the first reforming reactor to the catalyst in the fourth reforming reactor is 1 (1.4-1.6): (2.4-2.6): 4.9-5.1).
3. The optimized heavy naphtha processing according to claim 1, wherein the operating temperature of the depentanizer of step (3) is 200-220 ℃ and the operating pressure is 0.95-1.05MPa;
the operating temperature of the C6 removing tower is 140-160 ℃, and the operating pressure is 0.04-0.06MPa;
the operating temperature of the C4/C5 separating tower is 124-140 ℃, and the operating pressure is 1.15-1.35MPa.
4. The optimized heavy naphtha processing process of claim 1 wherein the lean solvent of step (4) is sulfolane, the lean solvent to C6 mass ratio is 2.5 to 5:1, and the extractive distillation column sensitivity plate operating temperature is 120 ± 10 ℃.
5. The optimized heavy naphtha processing process of claim 1, wherein the vacuum distillation pressure of the solvent recovery column of step (5) is-0.034 ± 0.01MPa.
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| JPH0431495A (en) * | 1990-05-26 | 1992-02-03 | Idemitsu Kosan Co Ltd | Method of reforming heavy naphtha |
| CN101570698A (en) * | 2008-04-29 | 2009-11-04 | 中国石油化工股份有限公司 | Method for catalyzing and transforming naphtha |
| CN102010746A (en) * | 2009-07-09 | 2011-04-13 | 北京金伟晖工程技术有限公司 | Reforming system and method for increasing aromatic hydrocarbons by naphtha |
| US11326112B1 (en) * | 2021-01-07 | 2022-05-10 | Saudi Arabian Oil Company | Integrated hydrocracking/adsorption and aromatic recovery complex to utilize the aromatic bottoms stream |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0431495A (en) * | 1990-05-26 | 1992-02-03 | Idemitsu Kosan Co Ltd | Method of reforming heavy naphtha |
| CN101570698A (en) * | 2008-04-29 | 2009-11-04 | 中国石油化工股份有限公司 | Method for catalyzing and transforming naphtha |
| CN102010746A (en) * | 2009-07-09 | 2011-04-13 | 北京金伟晖工程技术有限公司 | Reforming system and method for increasing aromatic hydrocarbons by naphtha |
| US11326112B1 (en) * | 2021-01-07 | 2022-05-10 | Saudi Arabian Oil Company | Integrated hydrocracking/adsorption and aromatic recovery complex to utilize the aromatic bottoms stream |
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