CN112225633A - Production method of normal hexane containing heptane raw material - Google Patents
Production method of normal hexane containing heptane raw material Download PDFInfo
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- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 title claims abstract description 142
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 title claims abstract description 138
- 239000002994 raw material Substances 0.000 title claims abstract description 63
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 25
- AFABGHUZZDYHJO-UHFFFAOYSA-N 2-Methylpentane Chemical compound CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 claims abstract description 64
- 239000000047 product Substances 0.000 claims abstract description 42
- 239000003054 catalyst Substances 0.000 claims abstract description 30
- 238000006243 chemical reaction Methods 0.000 claims abstract description 26
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 26
- 239000001257 hydrogen Substances 0.000 claims abstract description 26
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 21
- 238000000034 method Methods 0.000 claims abstract description 21
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 17
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 10
- 238000000926 separation method Methods 0.000 claims abstract description 9
- 238000005520 cutting process Methods 0.000 claims abstract description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 6
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims abstract description 6
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims abstract description 6
- 239000000203 mixture Substances 0.000 claims abstract description 6
- 229930195735 unsaturated hydrocarbon Natural products 0.000 claims abstract description 6
- 238000005194 fractionation Methods 0.000 claims abstract description 4
- 150000002431 hydrogen Chemical class 0.000 claims description 9
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 8
- 238000002156 mixing Methods 0.000 claims description 6
- 238000009835 boiling Methods 0.000 claims description 4
- 239000011148 porous material Substances 0.000 claims description 4
- 238000003825 pressing Methods 0.000 claims description 2
- 238000010992 reflux Methods 0.000 description 11
- 238000005265 energy consumption Methods 0.000 description 7
- 239000007789 gas Substances 0.000 description 6
- 238000006477 desulfuration reaction Methods 0.000 description 4
- 230000023556 desulfurization Effects 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 238000003672 processing method Methods 0.000 description 2
- 239000007858 starting material Substances 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/74—Iron group metals
- B01J23/755—Nickel
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
- B01J35/61—Surface area
- B01J35/613—10-100 m2/g
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
- B01J35/61—Surface area
- B01J35/615—100-500 m2/g
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
- B01J35/63—Pore volume
- B01J35/633—Pore volume less than 0.5 ml/g
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
- C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
- C07C4/06—Catalytic processes
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the iron group metals or copper
- C07C2523/74—Iron group metals
- C07C2523/755—Nickel
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Abstract
A method for producing normal hexane containing heptane raw materials comprises the following steps: the high heptane content crude hexane is fully mixed with hydrogen and then exchanges heat with reaction products, the mixture is heated to the reaction temperature by a heat exchanger, and then enters a hydrogenation reactor loaded with a catalyst to carry out hydrofining reaction under the action of a hydrofining catalyst, so that aromatic hydrocarbons and unsaturated hydrocarbons in raw materials are removed; after the reaction, the product is subjected to gas-liquid separation by a low-pressure separator and then enters a fractionation system for fine cutting; the fractionating system comprises a deheptanizer, a light component removal tower, an isohexane removal tower and a n-hexane removal tower which are connected in sequence; and (3) separating most heptane in the crude hexane with high heptane content from the reaction product in a deheptanizer in a prefractionation mode, and then finely cutting the obtained mixed carbon six-component oil in a light component removal tower, an isohexane removal tower and an n-hexane removal tower to obtain high-content n-hexane and isohexane products. The method can obtain high-purity isohexane, n-hexane products and heptane products.
Description
Technical Field
The invention belongs to the technical field of petrochemical industry, and particularly relates to a method for processing n-hexane, in particular to a method for producing n-hexane containing a heptane raw material (the heptane content is less than 50%).
Background
The hexane oil is a petrochemical product with high added value and is widely applied to the industries of food, medicine, chemical industry, metal processing, electronic instruments and the like. In industrial production, the production usually requires pretreatment of raw materials, and then a series of processes such as continuous rectification are carried out to obtain qualified hexane oil products.
In recent years, due to the process adjustment of oil refining enterprises, the content of heavy components such as heptane and the like in the n-hexane raw material at the present stage is gradually increased, so that the processing load of the original n-hexane raw material is increased, and the process index requirement is difficult to meet. In order to produce qualified normal hexane and isohexane products, many enterprises adopt means of increasing the temperature of the tower bottom, increasing the reflux ratio and the like, but the production energy consumption is increased, and the high-purity isohexane and normal hexane products are difficult to obtain, so that the economic benefit is influenced.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides the n-hexane production method of the heptane-containing raw material, which can obtain high-purity isohexane, n-hexane products and heptane products.
In order to solve the technical problems, the invention adopts the following technical scheme: a method for producing normal hexane containing heptane raw material comprises the following steps:
(1) fully mixing a raw material containing heptane with hydrogen, then exchanging heat with a reaction product, heating to a reaction temperature through a heat exchanger, entering a hydrogenation reactor loaded with a catalyst, and carrying out a hydrofining reaction under the action of a hydrofining catalyst to remove aromatic hydrocarbons and unsaturated hydrocarbons in the raw material;
(2) after the reaction, the product is subjected to gas-liquid separation by a low-pressure separator and then enters a fractionation system for fine cutting; the fractionating system comprises a deheptanizer, a light component removing tower, an isohexane removing tower and a n-hexane removing tower which are connected in sequence; and (3) separating most heptane in the heptane-containing raw material in a prefractionation mode after the reaction product enters a deheptanizer, and then entering a light component removal tower, an isohexane removal tower and an n-hexane removal tower to finely cut the obtained mixed carbon six-component oil to obtain high-content n-hexane and isohexane products.
The specification of the raw material containing heptane is as follows: the initial boiling point is 20-60 ℃, the final boiling point is 90-150 ℃, and the density at 20 ℃ is 600-750 kg/m3And the heptane content is less than 50 percent (mass percentage content).
The process conditions of the hydrofining reaction are as follows: the reaction temperature is 140-300 ℃, the reaction pressure is 1.3-6.0 MPa, and the volume space velocity is 0.5-5.0 h-1The volume ratio of the hydrogen to the oil is 200-1500: 1.
The catalyst for carrying out the hydrofining reaction is a nickel catalyst, the appearance of the catalyst is spherical, and the specific surface area of the catalyst is 50-120 m2(iv) per gram, pore volume of 0.15-0.5 ml/g, bulk density: 0.6 +/-0.02 g/ml and radial compressive strength of 15-60N/grain. The catalyst has good effect on hydrogenation saturation and dearomatization of the crude hexane with high heptane content.
The invention relates to a method for producing normal hexane containing heptane raw material, which comprises the steps of mixing the raw material with hydrogen, carrying out heat exchange with a reaction product in a heat exchanger, heating the mixture by a feeding heater to a reaction temperature, entering a hydrogenation reactor, carrying out hydrofining reaction under the action of a catalyst, and removing impurities such as unsaturated hydrocarbon, aromatic hydrocarbon and the like in the raw material.
Due to the adoption of the technical scheme, the invention has the following advantages:
1. the normal hexane production method of the heptane-containing raw material has wide distillation range of the raw material, and different production schemes can be selected according to the heptane content in the raw material. Even when the heptane content in the raw materials is high, high-purity n-hexane and isohexane products can be obtained under low energy consumption, the n-hexane content in the separated n-hexane product can reach 60-90%, the isohexane content in the separated isohexane product is greater than 95%, the separation precision is high, and a good use basis is provided for the next step of recycling of the two materials.
2. According to the method for producing the normal hexane containing the heptane raw material, the catalyst is a nickel-based catalyst, the low-temperature activity, the stability and the regeneration performance of the nickel-based catalyst are good, the reaction condition is mild, the unsaturated hydrocarbon and aromatic hydrocarbon removal effect is good, and the requirement of long-period operation can be met.
3. According to the method for producing the normal hexane containing the heptane raw material, the raw material is not heated by the heating furnace, is mixed with hydrogen, exchanges heat with a reaction product, and is heated to the reaction temperature by the feeding heater, so that the energy consumption is low and the heat exchange efficiency is high.
4. The method for producing the normal hexane containing the heptane raw material has the advantages of simple production process, stable product quality and high economic efficiency.
5. The method is flexible in adjustment, can carry out collocation of different systems according to the content of heptane, effectively reduces energy consumption, and is specific: when the content of heptane in the raw materials is more than or equal to 20 percent, a deheptanizer is used, reaction products are subjected to gas-liquid separation and then enter the deheptanizer for prefractionation, most of heptane in the raw materials is removed, the obtained mixed carbon six-component oil enters a fractionating system for product fine cutting, products are obtained, and when the content of heptane in the raw materials is less than 20 percent, the deheptanizer is closed.
6. According to the normal hexane production method of the heptane-containing raw material, four products with different brands can be obtained, and the obtained normal hexane and isohexane have high contents: the content of normal hexane is 60-90%, and the content of isohexane is more than 95%.
Drawings
FIG. 1 is a schematic diagram showing the structure of an apparatus for processing n-hexane containing a heptane-containing raw material used in the examples;
in the figure: 1-raw product heat exchanger; 2-a feed heater; 3-a hydrogenation reactor; 4-a recycle hydrogen desulfurization reactor; 5-a reaction product cooler; 6-low pressure separator; 7-circulating hydrogen separation tank; 8-recycle hydrogen compressor; 9-deheptanizer; 10-light component removing tower; 11-deisohexanizer column; 12-n-hexane removal tower; 13-feedstock inlet (feed pipe); 14-fresh hydrogen inlet (feed line); 15-light fraction take-off line; 16-isohexane out of the plant line; 17-n-hexane is discharged from a device pipeline; 18-mixed heptane outlet device pipeline, 19-cooler, 20-reflux tank and 21-reflux pump.
Detailed Description
The present invention will be further described in detail with reference to the following examples; however, the following examples are merely illustrative, and the present invention is not limited to these examples.
The following are different embodiments corresponding to the specific processing method:
example 1
The properties of the raw materials are shown in Table 1.
TABLE 1 Properties of the raw materials 1
A method for producing normal hexane containing heptane raw material comprises the following steps:
step 1, mixing the raw material with hydrogen, then exchanging heat with a reaction product, heating to 172 ℃ by a heater, putting the mixture into a reactor to contact with a catalyst, and carrying out hydrofining reaction under the action of a hydrofining catalyst, wherein the catalyst is a Ni catalyst, the appearance of the catalyst is spherical, and the specific surface area of the catalyst is 50-90 m2(iv) per gram, pore volume of 0.15-0.3 ml/g, bulk density: 0.6 +/-0.02 g/ml and radial compressive strength of 24-38N/grain.
And 2, carrying out gas-liquid separation on the reaction product in a low-pressure separator, then, entering a deheptanizer for prefractionation, separating out most heptane in the reaction product, and finely cutting the obtained mixed carbon six-component oil in a light component removing tower, an isohexane removing tower and an n-hexane removing tower to obtain light components, isohexane, n-hexane and mixed heptane products.
The product properties are shown in Table 2.
Table 2 product properties 1
From the table, the process method of the application can obtain four products, and the product content is high.
The heptane content in the raw material was 23.8%, the processing method without deheptanizer was used as comparative example, and table 3 shows the product properties after processing the raw material of comparative example. The comparison example shows that when the heptane content is more than 20 percent without a deheptanizer, the n-hexane and isohexane content obtained after the raw materials are processed is not high, the separation precision of a fractionation system is low, and the product index requirement is difficult to meet. The method for producing the normal hexane containing the heptane raw material can process the crude hexane with high heptane content to obtain high-purity normal hexane and isohexane products.
TABLE 3 comparative example product Properties
Example 2
The starting materials are shown in Table 4.
Table 4 crude hexane properties of the starting material 2
A method for producing normal hexane containing heptane raw material comprises the following steps:
step 1, mixing the raw materials with hydrogenAfter mixing, the temperature is 136 ℃ after heat exchange with reaction products, the mixture is heated to 178 ℃ by a heater, the mixture enters a reactor and contacts with a catalyst, and the hydrofining reaction is carried out under the action of a hydrofining catalyst, wherein the catalyst is a Ni catalyst, the appearance of the catalyst is spherical, and the specific surface area of the catalyst is 50-90 m2(iv) per gram, pore volume of 0.15-0.3 ml/g, bulk density: 0.6 +/-0.02 g/ml and radial compressive strength of 24-38N/grain. .
And 2, performing gas-liquid separation on the reaction product in a low-pressure separator, then entering a deheptanizer for prefractionation, separating out most heptane in the reaction product, and finely cutting the obtained mixed carbon six-component oil in a light component tower, an n-hexane tower and an isohexane tower to obtain n-hexane, isohexane, light components and mixed heptane products.
The product properties are shown in Table 5.
TABLE 5 product Properties 2
The structure schematic diagram of the processing device adopted in the method for producing normal hexane containing a heptane raw material according to the embodiment of the application is shown in the attached drawing 1: the device comprises a heat exchanger 1, a heater 2, a hydrogenation reactor 3, a recycle hydrogen desulfurization reactor 4, a reaction product cooler 5, a low-pressure separator 6, a recycle hydrogen separating tank 7, a recycle hydrogen compressor 8, a deheptanizer 9, a light component removing tower 10, an isohexane removing tower 11 and an n-hexane removing tower 12, wherein a cooler 19, a reflux tank 20 and a reflux pump 21 are arranged on each tower top.
The raw material inlet 13 of the heat exchanger 1 is connected with a raw material pump (the raw material pump is conventional equipment, not shown in the figure, and mainly used for conveying raw materials to provide power), the raw material outlet of the heat exchanger 1 is connected with the inlet of the heater 2 through a pipeline, the outlet of the heater 2 is connected with the inlet of the hydrogenation reactor 3 through a pipeline, the outlet of the hydrogenation reactor 3 is connected with the product inlet of the heat exchanger 1 through a pipeline, the product outlet of the heat exchanger 1 is connected with the inlet of the reaction product cooler 5 through a pipeline, and the outlet of the reaction product cooler 5 is connected with the inlet of the low-pressure separator 6 through a pipeline.
The gas outlet of the low-pressure separator 6 is connected with the gas inlet of a circulating hydrogen separating tank 7, the gas outlet of the circulating hydrogen separating tank 7 is connected with the gas inlet of a circulating hydrogen compressor 8, a fresh hydrogen inlet 14 (communicated with an external hydrogen source to provide newly injected hydrogen for the system) is connected with the gas outlet pipeline of the circulating hydrogen compressor 8, the gas outlet of the circulating hydrogen compressor 8 is connected with the inlet of a circulating hydrogen desulfurization reactor 4, and the outlet of the circulating hydrogen desulfurization reactor 4 is connected with the outlet pipeline of a raw material pump;
as can be seen from the attached drawings, the oil outlet of the low-pressure separator 6 is divided into two paths: one is connected with a feed inlet of a deheptanizer 9, and the other is connected with a feed inlet of a light component removal tower 10; the bottom of the deheptanizer 9 is connected with a mixed heptane outlet device pipeline 18, the top of the deheptanizer 9 is connected with a feed inlet of a light component removal tower 10, the top of the light component removal tower 10 is connected with a light component outlet device pipeline 15, the bottom of the light component removal tower 10 is connected with a feed inlet of an isohexane removal tower 11, the top of the isohexane removal tower 11 is connected with an isohexane outlet device pipeline 16, the bottom of the isohexane removal tower 11 is connected with a feed inlet of an n-hexane removal tower 12, and the top of the n-hexane removal tower 12 is connected with an n-hexane 17 outlet device pipeline; the bottom of the n-hexane removal tower is connected with a mixed heptane outlet device pipeline 18 (namely mixed heptane is discharged from the bottoms of the deheptanizer and the n-hexane removal tower in the application);
in addition, as can be seen from fig. 1, the tops of the deheptanizer 9, the light component removal column 10, the isohexane removal column 11 and the n-hexane removal column 12 are respectively connected with a cooler 19 and a reflux tank 20 through pipelines, the cooler 19 is connected with the reflux tank 20 through a pipeline, the reflux tank 20 is connected with a reflux pump 21 through a pipeline, and the outlet of the reflux pump 21 is connected with two pipelines: one of the pipelines is connected with the top reflux line of the tower in which the pipeline is positioned, and the other pipeline is connected with the pipeline of the product outlet device (different towers correspond to different products).
The application production facility of crude hexane of high heptane content, its high heptane content raw materials are by raw materials product heat exchanger 1 and feeding heater 2 direct heating to reaction temperature, need not adopt the heating furnace, have saved equipment and have reduced the energy consumption.
The application the apparatus for producing of high heptane content crude hexane, the heat transfer medium of heat exchanger be raw materials and reaction product to make full use of self circulation heat heating reduces the energy consumption.
The application production device of crude hexane with high heptane content, its adjustment is nimble changeable, can set for different production schemes according to raw materials nature: the deheptanizer is used when the heptane content in the raw material is more than or equal to 20 percent, and the deheptanizer is closed when the heptane content in the raw material is less than 20 percent.
The application discloses a processingequipment who contains n-hexane of heptane raw materials, wherein deheptanizer 9, light component tower 10, deisohexanizer 11 and deisohexanizer 12 are the plate column, adopt compound hole microvalve high-efficient column plate.
In the application, the n-hexane processing device containing the heptane raw material is characterized in that a product discharging device pump is not arranged at the bottoms of the deheptanizer and the n-hexane remover, and the product is pressed against a self-pressing device, so that the energy consumption is saved.
The light component outlet device pipeline, the isohexane outlet device pipeline, the normal hexane outlet device pipeline and the mixed heptane outlet device pipeline respectively correspond to the separated light component, isohexane, normal hexane and mixed heptane.
Each pipeline of the present application may be provided in a plurality of numbers in the corresponding device or component, depending on the particular connected component or device.
Claims (7)
1. A method for producing normal hexane containing heptane raw material is characterized in that: which comprises the following steps:
(1) fully mixing the raw material with hydrogen, then exchanging heat with a reaction product, heating to a reaction temperature through a heat exchanger, entering a hydrogenation reactor loaded with a catalyst, carrying out a hydrofining reaction under the action of a hydrofining catalyst, and removing aromatic hydrocarbons and unsaturated hydrocarbons in the raw material;
(2) after the reaction, the product is subjected to gas-liquid separation by a low-pressure separator and then enters a fractionation system for fine cutting; the fractionating system comprises a deheptanizer, a light component removal tower, an isohexane removal tower and a n-hexane removal tower which are connected in sequence; and (3) separating most heptane in the crude hexane with high heptane content from the reaction product in a deheptanizer in a prefractionation mode, and then finely cutting the obtained mixed carbon six-component oil in a light component removal tower, an isohexane removal tower and an n-hexane removal tower to obtain high-content n-hexane and isohexane products.
2. The method of claim 1, wherein the n-hexane comprises a heptane-containing feedstock, the method further comprising: different production schemes are set according to the properties of raw materials: when the content of heptane in the raw material is more than or equal to 20 percent, the deheptanizer is used, and when the content of heptane in the raw material is less than 20 percent, the deheptanizer is closed.
3. The method of claim 1, wherein the n-hexane comprises a heptane-containing feedstock, the method further comprising: the specification of the high-heptane-content crude hexane is as follows: the initial boiling point is 20-60 ℃, the final boiling point is 90-150 ℃, the density at 20 ℃ is 600-750 kg/m3, and the heptane content is less than 50%.
4. The method of claim 1 for producing n-hexane from a heptane-containing feed stock, wherein: the process conditions of the hydrofining reaction are as follows: the reaction temperature is 140-300 ℃, the reaction pressure is 1.3-6.0 MPa, the volume space velocity is 0.5-5.0 h < -1 >, and the volume ratio of hydrogen to oil is 200-1500: 1.
5. The method of claim 1, wherein the n-hexane comprises a heptane-containing feedstock, the method further comprising: the catalyst for carrying out the hydrofining reaction is a nickel catalyst, the appearance of the catalyst is spherical, and the specific surface area of the catalyst is 50-120 m2(iv) per gram, pore volume of 0.15-0.5 ml/g, bulk density: 0.6 +/-0.02 g/ml and radial compressive strength of 15-60N/grain.
6. The method of claim 1, wherein the n-hexane comprises a heptane-containing feedstock, the method further comprising: the raw material is firstly mixed with hydrogen and then exchanges heat with a reaction product in a heat exchanger, the mixture is heated by a heater to the reaction temperature and then enters a hydrogenation reactor, and the hydrofining reaction is carried out under the action of a catalyst to remove unsaturated hydrocarbon and aromatic hydrocarbon in the raw material.
7. The method of claim 1 for producing n-hexane from a heptane-containing feed stock, wherein: the tower bottom products of the deheptanizer and the n-hexane remover are discharged by a self-pressing device.
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| CN112745881A (en) * | 2019-10-31 | 2021-05-04 | 内蒙古伊泰煤制油有限责任公司 | Fischer-Tropsch stable light hydrocarbon deep processing method |
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