CN114540080A - Multi-raw-material n-hexane production device and n-hexane product processing method - Google Patents

Multi-raw-material n-hexane production device and n-hexane product processing method Download PDF

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CN114540080A
CN114540080A CN202210262729.0A CN202210262729A CN114540080A CN 114540080 A CN114540080 A CN 114540080A CN 202210262729 A CN202210262729 A CN 202210262729A CN 114540080 A CN114540080 A CN 114540080A
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tower
pipe
side line
separation
hexane
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CN114540080B (en
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杨明辉
卫建军
王志华
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China Petroleum and Chemical Corp
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China Petroleum and Chemical Corp
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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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
    • 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
    • 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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
    • C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
    • 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
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4006—Temperature
    • 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
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4012—Pressure
    • 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
    • C10G2300/70—Catalyst aspects
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • General Chemical & Material Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The application discloses a multi-raw-material n-hexane production device, which comprises a separation tower, a hydrogenation reactor, a lightness-removing tower and a heavy-removing tower, wherein a first side line pipe A and a first side line pipe B are led out from a side line discharge port of the separation tower, a first bottom pipe A and a first bottom pipe B are led out from a tower bottom discharge port of the separation tower, and the first bottom pipe B and the first side line pipe A are both communicated with a feed inlet of the hydrogenation reactor; a discharge hole at the bottom of the hydrogenation reactor is communicated with a feed inlet of the lightness-removing column through a separation tank; a third side line pipe A and a third side line pipe B are led out from a side line discharge port of the lightness-removing column, and a column bottom discharge port of the lightness-removing column is communicated with a feed port of the heaving column; a fourth tower top discharge pipe A and a fourth tower top discharge pipe B which are respectively communicated with the food-grade additive tank and the medical-grade additive tank are led out from a tower top discharge hole of the de-heavy tower. The application also discloses a processing method of the n-hexane product. By using the method, nonaromatic oil or C5-C6 component oil can be used as a raw material, C6 components are collected, and n-hexane products of different varieties are produced.

Description

Multi-raw-material n-hexane production device and n-hexane product processing method
Technical Field
The invention relates to a multi-raw-material n-hexane production device and a processing method of n-hexane products.
Background
At present, non-aromatic oil produced by an extraction unit of a reforming device of an oil refining chemical industry enterprise is one of blending components of gasoline, and the added value of the product is not high. In addition, after normal and isomeric components of C5-C6 component oil in the middle of a light naphtha product produced by a hydrocracking device and a topped oil product produced by a reforming device in a refining enterprise are separated, normal oil is used as an ethylene device raw material, and isomeric oil is used as a gasoline blending component, so that the added value of the product is not high.
Under the background that chemical products tend to be increasingly advanced at present, light-component byproducts of the refinery device are directly used for blending gasoline or are delivered from factories for sale as conventional product forms such as ethylene materials and the like, so that the improvement of the overall economic benefit of a refinery and the promotion of the advanced development strategy of the products are not facilitated.
Disclosure of Invention
In order to improve the additional value of non-aromatic component oil and C5-C6 component oil, the application firstly discloses a multi-raw-material n-hexane production device which comprises a separation tower, a hydrogenation reactor, a light component removal tower and a heavy component removal tower, wherein a raw material inlet is formed in the side wall of the separation tower, two first side line pipes are led out from a first side line discharge hole in the side wall of the separation tower, the two first side line pipes are respectively a first side line pipe A and a first side line pipe B, the first side line pipe B is communicated with a non-aromatic blending gasoline pool, the first side line discharge hole is positioned at the upper side of the raw material inlet, and a first tower top discharge pipe at the tower top of the separation tower is communicated with the non-aromatic blending gasoline pool;
two first tower bottom pipes are led out from a first tower bottom discharge hole at the bottom of the separation tower, and are respectively a first tower bottom pipe A and a first tower bottom pipe B, wherein the first tower bottom pipe A is communicated with a non-aromatic blending gasoline pool; the first tower bottom pipe B and the first side line pipe A are both communicated with a second feeding hole in the top of the hydrogenation reactor through a feeding pump, a second tower bottom discharging hole in the bottom of the hydrogenation reactor is communicated with a separation tank, and a liquid discharging hole in the bottom of the separation tank is communicated with a third feeding hole in the side wall of the lightness-removing tower;
two third side line pipes are led out from a third side line discharge port on the side wall of the lightness-removing tower, the two third side line pipes are a third side line pipe A and a third side line pipe B respectively, wherein the third side line pipe A is communicated with the solvent tank, the third side line pipe B is communicated with the non-aromatic blending gasoline pool, the third side line discharge port is positioned at the upper side of the raw material inlet, a third tower top discharge pipe at the tower top of the lightness-removing tower is communicated with the non-aromatic blending gasoline pool, and a third tower bottom discharge port at the tower bottom of the lightness-removing tower is communicated with a fourth feed port on the side wall of the lightness-removing tower;
two fourth tower top discharging pipes are led out from a fourth tower top discharging hole in the tower top of the de-heavy tower, the two fourth tower top discharging pipes are respectively a fourth tower top discharging pipe A and a fourth tower top discharging pipe B, the fourth tower top discharging pipe A is communicated with the food grade additive tank, the fourth tower top discharging pipe B is communicated with the medical grade additive tank, two fourth tower bottom pipes are led out from a fourth tower bottom discharging hole in the tower bottom of the de-heavy tower, the two fourth tower bottom pipes are respectively a fourth tower bottom pipe A and a fourth tower bottom pipe B, the fourth tower bottom pipe A is communicated with the petroleum ether tank, and the fourth tower bottom pipe B is communicated with the non-aromatic blending gasoline pool.
The n-hexane production device can adopt non-aromatic component oil or C5-C6 component oil as raw materials, and collects C6 components in the raw materials to produce different n-hexane products. When non-aromatic oil is used as a raw material, crude C6 is collected from a discharge port of a first side line of a separation tower, when C5-C6 component oil is used as the raw material, crude C6 is collected from the bottom of the separation tower, then crude C6 is subjected to hydrogenation treatment and is subjected to two times of separation in a light component removal tower and a heavy component removal tower in sequence, and a normal hexane product is collected from the top of the heavy component removal tower, wherein when the non-aromatic oil is used as the raw material, more than 80.5 wt% of normal hexane is collected, and when the C5-C6 component oil is used as the raw material, 99.5 wt% of normal hexane is collected. The n-hexane production device can adapt to different raw materials, produce corresponding n-hexane products and improve the product additional value of non-aromatic component oil rich in C6 components or C5-C6 component oil.
By converting the gasoline component into the special oil component, the economic benefit of the device can be effectively improved, and the multipurpose development of the device is realized.
Specifically, in order to ensure that the C6 component in the raw material can be separated to the maximum extent when the raw material is non-aromatic oil, the theoretical plate number of the separation tower is 80-110, the feeding position is 10-20, and the first side line discharge port is positioned at 50-70. The number of the column plates was counted from bottom to top. Through the process, the raw materials required by the normal hexane reactor can be fully extracted, and the yield of the target product is improved.
The application further provides a processing method of the n-hexane product, non-aromatic component oil or C5-C6 component oil is used as a raw material, the n-hexane production device with any one of the raw materials is used for producing the n-hexane, the processing method comprises the steps of separating the raw material through a separation tower to obtain a C6 crude product, hydrogenating the C6 crude product through a hydrogenation reactor to obtain a saturated material, separating the saturated material to obtain a crude n-hexane, removing light components from the crude n-hexane through a light component removal tower, feeding the tower bottom material of the light component removal tower into a heavy component removal tower, and collecting the n-hexane from the tower top of the heavy component removal tower.
By the processing method, the reasonable configuration of main products and byproducts of the device can be realized, and the analysis results and the product yield of each component are ensured. The benzene and the phenyl in the C6 crude product are saturated by hydrogenation to form cyclane, i.e. debenzolization reaction is carried out. When non-aromatic oil is used as a raw material, the yield of the n-hexane product is more than or equal to 50 percent relative to the n-hexane content in the raw material. When the C5-C6 component oil is used as a raw material, the yield of n-hexane product energy is more than or equal to 93 percent relative to the n-hexane content in the raw material.
Specifically, when the raw material is non-aromatic oil, the processing method comprises the following steps:
(1.1) separating non-aromatic oil by a separation tower, feeding a first tower top light component A of the separation tower into a non-aromatic blending gasoline pool through a first tower top discharge pipe, collecting a C6 crude product through a first side pipeline A, and feeding a first tower bottom oil A of the separation tower into the non-aromatic blending gasoline pool through a first tower bottom pipe A;
(1.2) mixing the crude product of C6 with hydrogen to form a hydrogenation raw material in a gas-liquid mixed phase state, feeding the hydrogenation raw material into a hydrogenation reactor, carrying out aromatic saturation reaction to obtain a saturated material, separating the saturated material by a separation tank to obtain crude hydrogen and crude n-hexane in a liquid phase, wherein the crude hydrogen is recycled by a recycle hydrogen compressor;
(1.3) the crude n-hexane enters a lightness-removing tower through a third feed inlet for separation, a light component A at the third tower top of the lightness-removing tower enters a non-aromatic blending gasoline pool through a discharge pipe at the third tower top, a vegetable oil extraction solvent oil is extracted from a third side pipeline A of the lightness-removing tower, and a third tower bottom material A of the lightness-removing tower enters a weight-removing tower through a fourth feed inlet for separation;
the light component A at the fourth tower top of the heavy component removal tower is extracted by a fourth tower top discharge pipe A to obtain n-hexane with the weight percent of more than 80.5 percent, and the tower bottom material of the heavy component removal tower is extracted as petroleum ether; more than 80.5 wt% n-hexane can be used as a food grade additive;
when the raw material is C5-C6 component oil, the processing method comprises the following steps:
(2.1) separating the C5-C6 component oil by a separation tower, feeding a first tower top light component B of the separation tower into a non-aromatic blending gasoline pool through a first tower top discharge pipe, collecting a first side line light component B through a first side line pipe B, feeding the first side line light component B into the non-aromatic blending gasoline pool, and taking first tower bottom oil B of the separation tower as a C6 crude product;
(2.2) mixing the crude product of C6 with hydrogen to form a hydrogenation raw material in a gas-liquid mixed phase state, feeding the hydrogenation raw material into a hydrogenation reactor, carrying out aromatic saturation reaction to obtain a saturated material, separating the saturated material by a separation tank to obtain crude hydrogen and crude n-hexane in a liquid phase, wherein the crude hydrogen is recycled by a recycle hydrogen compressor;
(2.3) the crude n-hexane enters a lightness-removing tower through a third feeding hole for separation, a third tower top light component B of the lightness-removing tower enters a non-aromatic blending gasoline pool through a third tower top discharging pipe, a third side pipeline B of the lightness-removing tower collects a third side line light component B, the third side line light component B enters the non-aromatic blending gasoline pool, and a third tower bottom material B of the lightness-removing tower enters a heavy-removing tower through a fourth feeding hole for separation;
and (3) extracting 99.5 wt% of normal hexane from a fourth tower top light component B of the de-heavy tower through a fourth tower top discharge pipe B, feeding the tower bottom material of the de-heavy tower into a non-aromatic blending gasoline pool, and using the 99.5 wt% of normal hexane as a pharmaceutical grade additive.
In this application, utilize above-mentioned n-hexane apparatus for producing, adopt different raw materials in order to produce the n-hexane of different piece qualities, owing to adopted same set of device, can reduce the investment of equipment. The non-aromatic oil rich in C6 components or the C5-C6 component oil is used as a raw material, so that the product added value of the non-aromatic oil or the C5-C6 component oil can be effectively improved, wherein the non-aromatic oil is produced by an extraction unit of a continuous reforming device, and the C5-C6 component oil is normal oil obtained by separating normal and isomeric components from at least one of a topping oil produced by a pre-hydrogenation fractionating tower of the continuous reforming device and a light naphtha produced by a naphtha fractionating tower top of a hydrocracking device. Namely, the component oil C5-C6 is normal oil obtained by separating normal and isomeric components from the topping oil produced by a pre-hydrogenation fractionating tower of a continuous reforming device, or is normal oil obtained by separating normal and isomeric components from light naphtha produced at the top of a naphtha fractionating tower of a hydrocracking device, or is mixed oil of the two normal oils.
By using non-aromatic oil or C5-C6 oil as the processing raw material, high-value n-hexane products with different purities can be extracted, and byproducts can be reasonably utilized as gasoline blend oil and ethylene blend raw materials. When non-aromatic oil is used as a raw material, the yield of the vegetable oil extraction solvent oil is more than or equal to 43 percent relative to the content of normal hexane in the raw material, so that the total yield of the vegetable oil extraction solvent oil and the normal hexane product is more than or equal to 93 percent.
Specifically, in order to ensure that the C6 component can be separated to the maximum extent under different types of raw materials, in the step (1.1), the operation process parameters of the separation tower are as follows: the temperature at the top of the tower ranges from 81 to 83 ℃, the temperature at the bottom of the tower ranges from 156 to 165 ℃, the reflux ratio ranges from 1.70 to 1.90, and the pressure at the top of the tower ranges from 0.13 to 0.15 MPa;
in the step (2.1), the operation process parameters of the separation tower are as follows: the temperature of the top of the tower is 60-62 ℃, the temperature of the bottom of the tower is 96-98 ℃, the reflux ratio is 0.65-0.68, and the pressure of the top of the tower is 0.130-0.135 MPa.
Through adjustment within a certain interval range, allowance can be reserved for device operation parameters under the condition that main products are qualified, and fluctuation resistance is improved.
Further, because the raw materials are different and the crude C6 product contains different specific components, in order to better adapt to the crude C6 product collected from different raw materials, in step (1.2), the operating process parameters of the hydrogenation reactor are as follows: the inlet temperature is 70-200 ℃, the outlet temperature is 70-210 ℃, and the reaction pressure is 1.2-1.8 MPa;
in the step (2.2), the operating process parameters of the hydrogenation reactor are as follows: the inlet temperature is 70-230 ℃, the outlet temperature is 70-240 ℃, and the reaction pressure is 1.2-1.8 MPa.
The service life of the catalyst can be fully developed by adjusting the reaction temperature and the reaction pressure, the yield of the target product is ensured, and the benefit maximization of the device is ensured.
Specifically, in the step (1.3), the operating process parameters of the light component removal tower are as follows: the temperature at the top of the tower is 70-72 ℃, the temperature at the bottom of the tower is 98-99 ℃, the reflux ratio is 1.9-2.1, and the pressure at the top of the tower is 0.04-0.05 MPa;
in the step (2.3), the operation process parameters of the light component removal tower are as follows: the temperature at the top of the tower is 77-79 ℃, the temperature at the bottom of the tower is 90-93 ℃, the reflux ratio is 1.9-2.1, and the pressure at the top of the tower is 0.04-0.05 MPa.
By maintaining the reaction parameters, the separation effect of the rectifying tower can be ensured, and the product yield is maximized.
Specifically, in the step (1.3), the operation process parameters of the de-heavy tower are as follows: the temperature at the top of the tower is 80-81 ℃, the temperature at the bottom of the tower is 108-110 ℃, the reflux ratio is 6.2-6.8, and the pressure at the top of the tower is 0.04-0.05;
in the step (2.3), the operation process parameters of the de-heavy tower are as follows: the temperature at the top of the tower is 80-81 ℃, the temperature at the bottom of the tower is 92-94, the reflux ratio is 7-7.2, and the pressure at the top of the tower is 0.04-0.05.
By maintaining the reaction parameters, the separation effect of the rectifying tower can be ensured, the product yield is maximized, and a certain fluctuation interval is allowed.
In this application, the reflux ratio is the ratio of the amount of reflux to the amount of feed.
Specifically, in order to make hydrogenation smoothly proceed, the hydrogenation catalyst in the hydrogenation reactor is FHJ-2 catalyst. The catalyst can ensure the removal efficiency of benzene in the raw materials and simultaneously ensure the running time of a single overhaul period of the device.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present invention.
Detailed Description
A multi-raw-material n-hexane production device comprises a separation tower 10, a hydrogenation reactor 20, a lightness-removing tower 30 and a heaving removing tower 40, wherein a raw material inlet 11 is formed in the side wall of the separation tower 10, a first feeding pipe 111 and a second feeding pipe 113 are connected to the raw material inlet, a first feeding valve 112 is installed on the first feeding pipe 111, and a second feeding valve 114 is installed on the second feeding pipe 113. Two first side spool pipes are led out from a first side line discharge port 13 on the side wall of the separation tower 10, the two first side spool pipes are a first side spool pipe A131 and a first side spool pipe B133 respectively, wherein the first side spool pipe B is communicated with a non-aromatic blending gasoline pool, the first side line discharge port is positioned at the upper side of a raw material inlet, a first tower top discharge port 12 of the separation tower 10 is connected with a first return tank 121, the first return tank 121 is communicated with the separation tower through a first return pipe 122, a first tower top discharge pipe 123 is further connected to the bottom of the first return tank 121, and the first tower top discharge pipe is communicated with the non-aromatic blending gasoline pool.
A first side line switching valve a132 is attached to the first side line pipe a131, and a first side line switching valve B134 is attached to the first side line pipe B133.
Two first tower bottom pipes are led out from a first tower bottom discharge hole 14 at the tower bottom of the separation tower 10, wherein the two first tower bottom pipes are a first tower bottom pipe A141 and a first tower bottom pipe B143 respectively, and the first tower bottom pipe A is communicated with a non-aromatic blending gasoline pool. The first tower bottom pipe B and the first side pipe A are both communicated with the inlet of the feeding pump 61. A first column bottom switching valve a142 is attached to the first column bottom a141, and a first column bottom switching valve B144 is attached to the first column bottom B143.
In this example, the number of theoretical plates of the separation column was 100, the feed position was 13 th, and the first side line outlet was located at 65. The number of the plates of the separation column was counted from bottom to top.
An outlet pipe 211 of the feed pump sequentially passes through a refrigerant channel of the heat exchanger 62 and the heater 64 and then is communicated with a second feed inlet 21 at the top of the hydrogenation reactor 20, a hydrogenation pipe 212 is connected to the outlet pipe 211, and the connection point of the hydrogenation pipe and the outlet pipe is positioned between the heat exchanger 62 and the feed pump. The heat exchanger 62 is a plate heat exchanger, and the heater 64 is a heat conducting oil heater.
The second bottom discharge port 22 at the bottom of the hydrogenation reactor 20 is connected with a hydrogenation discharge pipe 221, the hydrogenation discharge pipe 221 sequentially passes through a heating medium channel of the heat exchanger 62 and the cooler 63 and then is communicated with the tank inlet 51 of the knockout drum 50, the top of the knockout drum is connected with a hydrogen discharge pipe 52, and the liquid discharge port 53 at the bottom of the knockout drum is communicated with the third feed port 31 on the side wall of the lightness-removing column 30.
Two third side line pipes are led out from a third side line discharge port 33 on the side wall of the lightness-removing tower 30, the two third side line pipes are a third side line pipe A331 and a third side line pipe B333 respectively, wherein the third side line pipe A is communicated with the solvent tank, the third side line pipe B is communicated with the non-aromatic blending gasoline pool, and the third side line discharge port is positioned at the upper side of the raw material inlet. A third side line switching valve a332 is attached to the third side line pipe a331, and a third side line switching valve B334 is attached to the third side line pipe B333.
A third reflux tank 321 is connected to a third top discharge port 32 of the light component removal tower 30, the third reflux tank 321 is communicated with the light component removal tower through a third reflux pipe 322, a third top discharge pipe 323 is further connected to the bottom of the third reflux tank 321, and the first top discharge pipe is communicated with a non-aromatic blending gasoline pool. The third bottom outlet 34 of the light component removal tower is communicated with a fourth inlet 41 on the side wall of the heavy component removal tower 40.
A fourth reflux tank 421 is connected to a fourth top discharge port 42 at the top of the de-heavy tower 40, the fourth reflux tank 421 is communicated with the de-heavy tower through a fourth reflux pipe 422, two fourth top discharge pipes are led out from the bottom of the fourth reflux tank 421, the four fourth top discharge pipes are a fourth top discharge pipe A424 and a fourth top discharge pipe B426, the fourth top discharge pipe A is communicated with a food grade additive tank, and the fourth top discharge pipe B is communicated with a medical grade additive tank. A fourth column top switching valve a425 is installed in the fourth column top outlet a, and a fourth column top switching valve B427 is installed in the fourth column top outlet B.
Two fourth tower bottom pipes are led out from a fourth tower bottom discharge hole 43 at the bottom of the de-heavy tower 40, and are respectively a fourth tower bottom pipe A431 and a fourth tower bottom pipe B433, wherein the fourth tower bottom pipe A is communicated with the petroleum ether tank, and the fourth tower bottom pipe B is communicated with the non-aromatic blending gasoline pool. A fourth column switching valve a432 is installed in the fourth column pipe a431, and a fourth column switching valve B434 is installed in the fourth column pipe B433.
The following is a description of the method of processing the n-hexane product.
The following first describes a processing method for producing n-hexane by using non-aromatic component oil as a raw material, wherein the non-aromatic component oil is produced by an extraction unit of a continuous reforming device, the processing method is carried out by using the multi-raw-material n-hexane production device, and the processing method comprises the following specific steps:
(1.1) the first feed valve 112 is opened, the second feed valve 114 is closed, and the non-aromatic oil 911 is fed into the separation column through the first feed pipe 111 to be separated.
The overhead gas of the separation tower is condensed and then enters a first reflux tank 121, part of the condensate returns to the separation tower, part of the condensate becomes a first tower top light component A920, and the first tower top light component A920 enters a non-aromatic blending gasoline pool through a first tower top discharge pipe 123.
The first side line switching valve B134 is closed, the first side line switching valve A132 is opened, and crude C6 is collected from the first side line discharge port 13. The first tower bottom switching valve B144 is closed, and the first tower bottom switching valve A142 is opened, so that the first tower bottom oil A940 of the separation tower enters the non-aromatic and gasoline pool through the first tower bottom pipe A.
(1.2) mixing the crude product of C6 with hydrogen to form a hydrogenation raw material in a gas-liquid mixed phase state, heating the hydrogenation raw material by a heat exchanger 62 and a heater 64 in sequence under the drive of a feed pump 61, then feeding the hydrogenation raw material into a hydrogenation reactor 20 through a second feed inlet 21 to carry out hydrogenation reaction, carrying out aromatic saturation reaction on benzene in the hydrogenation reactor to obtain a saturated material, discharging the saturated material through a discharge outlet 22 at the bottom of a second tower, cooling the saturated material by the heat exchanger 62 and a cooler 63 in sequence, feeding the cooled saturated material into a separation tank 50, separating the saturated material into crude hydrogen 950 and crude n-hexane in the separation tank, discharging the crude hydrogen 950 through a hydrogen discharge pipe 52, and adjusting the crude hydrogen to be recycled through a recycle hydrogen compressor.
(1.3) the crude n-hexane enters a lightness-removing column 30 through a third feeding port 31 for separation, overhead gas of the lightness-removing column is condensed and then enters a third reflux tank 321, part of condensate returns to the lightness-removing column, part of condensate becomes a light component A at the top of the third column, and the light component A at the top of the third column enters a non-aromatic blending gasoline pool. The third side line switching valve B334 is closed, the third side line switching valve A332 is opened, and the vegetable oil extraction solvent oil 971 is extracted from the third side line pipe A of the lightness-removing column. The bottom material A of the third tower of the light component removal tower enters the heavy component removal tower 40 through a fourth feed inlet 41 for separation.
The overhead gas of the de-heavy tower is condensed and then enters a fourth reflux tank 421, part of the condensate returns to the de-heavy tower, a fourth tower top switching valve B427 is closed, a fourth tower top switching valve A425 is opened, and part of the condensate is extracted from a fourth tower top discharge pipe A to form a fourth tower top light component A981, the fourth tower top light component A981 is used as n-hexane with the weight percent being more than 80.5, and the n-hexane with the weight percent being more than 80.5 can be used as a food grade additive.
The fourth column bottom switching valve B434 is closed, the fourth column bottom switching valve A432 is opened, and the column bottom material of the de-heavy column is extracted from the fourth column bottom pipe A431 as the petroleum ether 991.
In this embodiment, in step (1.1), the operating process parameters of the separation column are as follows: the temperature of the top of the tower ranges from 81 to 83 ℃, the temperature of the bottom of the tower ranges from 158 to 161 ℃, the reflux ratio ranges from 1.70 to 1.90, and the pressure of the top of the tower ranges from 0.13 to 0.15 MPa. In the step (1.2), the operating process parameters of the hydrogenation reactor are as follows: the inlet temperature is 90-100 ℃, the outlet temperature is 110-120 ℃, and the reaction pressure is 1.5-1.6 MPa. In the step (1.3), the operation process parameters of the light component removal tower are as follows: the temperature at the top of the tower is 70-72 ℃, the temperature at the bottom of the tower is 98-99 ℃, the reflux ratio is 1.9-2.1, and the pressure at the top of the tower is 0.04-0.05 MPa. In the step (1.3), the operation process parameters of the de-heavy tower are as follows: the temperature at the top of the tower is 80-81 ℃, the temperature at the bottom of the tower is 108-110 ℃, the reflux ratio (the ratio of reflux to feed) is 6.2-6.8, and the pressure at the top of the tower is 0.04-0.05. The hydrogenation catalyst in the hydrogenation reactor is FHJ-2 catalyst. The raw material components and the product components in this example are shown in tables 1 and 2.
TABLE 1 non-aromatic oil feedstock and product compositions
Figure BDA0003551206420000071
TABLE 2 vegetable oil extraction solvent oil composition
Figure BDA0003551206420000072
Figure BDA0003551206420000081
In this example, the yield of 86% pure n-hexane was 51.1% and the yield of vegetable oil-extracted solvent oil was 44.3%, based on n-hexane in the non-aromatic oil, and the total yield of both was 95.4%. In the embodiment, the distillation range of the vegetable oil extraction solvent oil is between 61 and 76 ℃ in normal pressure distillation analysis, while the lightness-removing column designed by the patent is operated at the pressure of 0.04MPa, the temperature at the top of the column is between 70 and 72 ℃, and the distillation range intervals of substances are different under different pressures.
The following description is provided for a processing method for producing normal hexane by using C5-C6 component oil as a raw material, wherein the C5-C6 component oil is normal oil obtained by separating normal isomeric components from topped oil produced by a pre-hydrogenation fractionating tower of a continuous reforming device, the processing method is carried out by using the multi-raw-material normal hexane production device, and the processing method comprises the following specific steps:
(2.1) the first feed valve 112 is closed and the second feed valve 114 is opened, and the component oil 912 from C5 to C6 is fed into the separation column through the second feed pipe 113 to be separated.
The overhead gas of the separation tower is condensed and then enters a first reflux tank 121, part of the condensate returns to the separation tower, part of the condensate becomes a first tower top light component B, and the first tower top light component B enters a non-aromatic blending gasoline pool through a first tower top discharge pipe 123.
And (3) opening a first side line switching valve B134, closing a first side line switching valve A132, collecting a first side line light component B930 from the first side line pipe B, and enabling the first side line light component B to enter a non-aromatic blending gasoline pool, wherein the first bottom oil B of the separation tower is used as a crude product C6.
(2.2) mixing the crude product of C6 with hydrogen to form a hydrogenation raw material in a gas-liquid mixed phase state, heating the hydrogenation raw material by a heat exchanger 62 and a heater 64 in sequence under the drive of a hydrogenation raw material feeding pump 61, then feeding the hydrogenation raw material into a hydrogenation reactor 20 through a second feeding hole 21 to perform hydrogenation reaction, performing aromatic saturation reaction on benzene in the hydrogenation reactor to obtain a saturated material, discharging the saturated material through a bottom discharge hole 22 of a second tower, cooling the saturated material by the heat exchanger 62 and a cooler 63 in sequence, feeding the cooled saturated material into a separation tank 50, separating the saturated material into crude hydrogen 950 and crude n-hexane in the separation tank, discharging the crude hydrogen 950 through a hydrogen discharge pipe 52, and adjusting the crude hydrogen 950 to be recycled through a recycle hydrogen compressor.
(2.3) the crude n-hexane enters the lightness-removing column 30 through a third feeding hole for separation, overhead gas of the lightness-removing column is condensed and then enters a third reflux tank 321, part of condensate returns to the lightness-removing column, part of condensate becomes a light component B at the top of the third column, and the light component B at the top of the third column enters a non-aromatic blending gasoline pool through a discharge pipe at the top of the third column.
And opening a third side line switching valve B334, closing the third side line switching valve A332, collecting a third side line light component B972 from a third side line pipe B of the lightness-removing tower, feeding the third side line light component B into a non-aromatic blending gasoline pool, and feeding a third tower bottom material B of the lightness-removing tower into a heavy-removing tower 40 through a fourth feeding hole 41 for separation.
The overhead gas of the de-heavy tower is condensed and then enters a fourth reflux tank 421, part of the condensate returns to the de-heavy tower, a fourth tower top switching valve B427 is opened, a fourth tower top switching valve A425 is closed, and part of the condensate is extracted from a fourth tower top discharge pipe B to form a fourth tower top light component B982, the fourth tower top light component B982 is used as 99.5 wt% of n-hexane, and the 99.5 wt% of n-hexane can be used as a pharmaceutical grade additive.
And (3) opening a fourth tower bottom switching valve B434, closing a fourth tower bottom switching valve A432, and allowing tower bottom materials of the de-heavy tower to enter a non-aromatic blending gasoline pool through a fourth tower bottom pipe B.
In this embodiment, in the step (2.1), the operating process parameters of the separation tower are as follows: the temperature of the top of the tower is 60-62 ℃, the temperature of the bottom of the tower is 96-98 ℃, the reflux ratio is 0.65-0.68, and the pressure of the top of the tower is 0.130-0.135 MPa. In the step (2.2), the operating process parameters of the hydrogenation reactor are as follows: the inlet temperature is 100-110 ℃, the outlet temperature is 110-120 ℃, and the reaction pressure is 1.5-1.6 MPa. In the step (2.3), the operation process parameters of the light component removal tower are as follows: the temperature at the top of the tower is 77-79 ℃, the temperature at the bottom of the tower is 90-93 ℃, the reflux ratio is 1.9-2.1, and the pressure at the top of the tower is 0.04-0.05 MPa. In the step (2.3), the operation process parameters of the de-heavy tower are as follows: the temperature at the top of the tower is 80-81 ℃, the temperature at the bottom of the tower is 92-94 ℃, the reflux ratio is 7-7.2, and the pressure at the top of the tower is 0.04-0.05 MPa. The hydrogenation catalyst in the hydrogenation reactor is FHJ-2 catalyst. The raw material components and the product components in this example are shown in Table 3.
TABLE 3C5-C6 component oils raw materials and product compositions
Figure BDA0003551206420000091
In this example, the yield of 99.5% pure n-hexane was 93.6% based on n-hexane in the C5-C6 component oil.
It is understood that in other embodiments, the C5-C6 component oil may be a normal oil obtained by separating normal and isomeric components of light naphtha produced from the top of a naphtha fractionator of a hydrocracking unit, or a mixture of a normal oil obtained by separating normal and isomeric components of a topped oil from a pre-hydrogenation fractionator of a continuous reforming unit and a normal oil obtained by separating normal and isomeric components of light naphtha produced from the top of a naphtha fractionator of a hydrocracking unit.

Claims (9)

1. The multi-raw-material n-hexane production device is characterized by comprising a separation tower, a hydrogenation reactor, a lightness-removing tower and a heaving removing tower, wherein a raw material inlet is formed in the side wall of the separation tower, two first side line pipes are led out from a first side line discharge port in the side wall of the separation tower, the two first side line pipes are respectively a first side line pipe A and a first side line pipe B, the first side line pipe B is communicated with a non-aromatic blending gasoline pool, the first side line discharge port is positioned on the upper side of the raw material inlet, and a first tower top discharge pipe at the tower top of the separation tower is communicated with the non-aromatic blending gasoline pool;
two first tower bottom pipes are led out from a first tower bottom discharge hole at the bottom of the separation tower, and are respectively a first tower bottom pipe A and a first tower bottom pipe B, wherein the first tower bottom pipe A is communicated with a non-aromatic blending gasoline pool; the first tower bottom pipe B and the first side line pipe A are both communicated with a second feeding hole in the top of the hydrogenation reactor through a feeding pump, a second tower bottom discharging hole in the bottom of the hydrogenation reactor is communicated with a separation tank, and a liquid discharging hole in the bottom of the separation tank is communicated with a third feeding hole in the side wall of the lightness-removing tower;
two third side line pipes are led out from a third side line discharge port on the side wall of the lightness-removing tower, the two third side line pipes are a third side line pipe A and a third side line pipe B respectively, wherein the third side line pipe A is communicated with the solvent tank, the third side line pipe B is communicated with the non-aromatic blending gasoline pool, the third side line discharge port is positioned at the upper side of the raw material inlet, a third tower top discharge pipe at the tower top of the lightness-removing tower is communicated with the non-aromatic blending gasoline pool, and a third tower bottom discharge port at the tower bottom of the lightness-removing tower is communicated with a fourth feed port on the side wall of the lightness-removing tower;
two fourth tower top discharging pipes are led out from a fourth tower top discharging hole in the tower top of the de-heavy tower, the two fourth tower top discharging pipes are respectively a fourth tower top discharging pipe A and a fourth tower top discharging pipe B, the fourth tower top discharging pipe A is communicated with the food grade additive tank, the fourth tower top discharging pipe B is communicated with the medical grade additive tank, two fourth tower bottom pipes are led out from a fourth tower bottom discharging hole in the tower bottom of the de-heavy tower, the two fourth tower bottom pipes are respectively a fourth tower bottom pipe A and a fourth tower bottom pipe B, the fourth tower bottom pipe A is communicated with the petroleum ether tank, and the fourth tower bottom pipe B is communicated with the non-aromatic blending gasoline pool.
2. The apparatus for producing n-hexane according to claim 1, wherein the number of theoretical plates of the separation column is 80 to 110, the feed position is 10 to 20, and the first side line outlet is located at 50 to 70.
3. A method for processing an n-hexane product is characterized in that non-aromatic component oil or C5-C6 component oil is used as a raw material, and an n-hexane production device with multiple raw materials as claimed in claim 1 or 2 is used for producing the n-hexane.
4. A process according to claim 3, wherein when the feedstock is a non-aromatic oil, the process comprises the steps of:
(1.1) separating non-aromatic oil by a separation tower, feeding a first tower top light component A of the separation tower into a non-aromatic blending gasoline pool through a first tower top discharge pipe, collecting a C6 crude product through a first side pipeline A, and feeding a first tower bottom oil A of the separation tower into the non-aromatic blending gasoline pool through a first tower bottom pipe A;
(1.2) mixing the crude C6 product with hydrogen to form a gas-liquid mixed phase hydrogenation raw material, feeding the hydrogenation raw material into a hydrogenation reactor, carrying out aromatic saturation reaction to obtain a saturated material, separating the saturated material by a separation tank to obtain crude hydrogen and crude n-hexane in a liquid phase, wherein the crude hydrogen is recycled by a recycle hydrogen compressor;
(1.3) the crude n-hexane enters a lightness-removing tower through a third feed inlet for separation, a light component A at the third tower top of the lightness-removing tower enters a non-aromatic blending gasoline pool through a discharge pipe at the third tower top, a vegetable oil extraction solvent oil is extracted from a third side pipeline A of the lightness-removing tower, and a third tower bottom material A of the lightness-removing tower enters a weight-removing tower through a fourth feed inlet for separation;
the light component A at the fourth tower top of the heavy component removing tower is extracted by a discharge pipe A at the fourth tower top to obtain n-hexane with the weight percent of more than 80.5 percent, and the tower bottom material of the heavy component removing tower is extracted as petroleum ether;
when the raw material is C5-C6 component oil, the processing method comprises the following steps:
(2.1) separating the C5-C6 component oil by a separation tower, feeding a first tower top light component B of the separation tower into a non-aromatic blending gasoline pool through a first tower top discharge pipe, collecting a first side line light component B through a first side line pipe B, feeding the first side line light component B into the non-aromatic blending gasoline pool, and taking first tower bottom oil B of the separation tower as a C6 crude product;
(2.2) mixing the crude product of C6 with hydrogen to form a hydrogenation raw material in a gas-liquid mixed phase state, feeding the hydrogenation raw material into a hydrogenation reactor, carrying out aromatic saturation reaction to obtain a saturated material, separating the saturated material by a separation tank to obtain crude hydrogen and crude n-hexane in a liquid phase, wherein the crude hydrogen is recycled by a recycle hydrogen compressor;
(2.3) the crude n-hexane enters a lightness-removing tower through a third feeding hole for separation, a third tower top light component B of the lightness-removing tower enters a non-aromatic blending gasoline pool through a third tower top discharging pipe, a third side pipeline B of the lightness-removing tower collects a third side line light component B, the third side line light component B enters the non-aromatic blending gasoline pool, and a third tower bottom material B of the lightness-removing tower enters a heavy-removing tower through a fourth feeding hole for separation;
and (3) extracting 99.5 wt% of normal hexane from a fourth tower top light component B of the de-heavy tower through a fourth tower top discharge pipe B, and feeding the tower bottom material of the de-heavy tower into a non-aromatic blending gasoline pool.
5. The processing method according to claim 4,
in the step (1.1), the operation process parameters of the separation tower are as follows: the temperature at the top of the tower is 81-83 ℃, the temperature at the bottom of the tower is 156-165 ℃, the reflux ratio is 1.70-1.90, and the pressure at the top of the tower is 0.13-0.15 MPa;
in the step (2.1), the operation process parameters of the separation tower are as follows: the temperature of the top of the tower is 60-62 ℃, the temperature of the bottom of the tower is 96-98 ℃, the reflux ratio is 0.65-0.68, and the pressure of the top of the tower is 0.130-0.135 MPa.
6. The processing method according to claim 4,
in the step (1.2), the operating process parameters of the hydrogenation reactor are as follows: the inlet temperature is 70-200 ℃, the outlet temperature is 70-210 ℃, and the reaction pressure is 1.2-1.8 MPa;
in the step (2.2), the operating process parameters of the hydrogenation reactor are as follows: the inlet temperature is 70-230 ℃, the outlet temperature is 70-240 ℃, and the reaction pressure is 1.2-1.8 MPa.
7. The processing method according to claim 4,
in the step (1.3), the operation process parameters of the light component removal tower are as follows: the temperature at the top of the tower is 70-72 ℃, the temperature at the bottom of the tower is 98-99 ℃, the reflux ratio is 1.9-2.1, and the pressure at the top of the tower is 0.04-0.05 MPa;
in the step (2.3), the operation process parameters of the light component removal tower are as follows: the temperature at the top of the tower is 77-79 ℃, the temperature at the bottom of the tower is 90-93 ℃, the reflux ratio is 1.9-2.1, and the pressure at the top of the tower is 0.04-0.05 MPa.
8. The processing method according to claim 4,
in the step (1.3), the operation process parameters of the de-heavy tower are as follows: the temperature at the top of the tower is 80-81 ℃, the temperature at the bottom of the tower is 108-110 ℃, the reflux ratio is 6.2-6.8, and the pressure at the top of the tower is 0.04-0.05 MPa;
in the step (2.3), the operation process parameters of the de-heavy tower are as follows: the temperature at the top of the tower is 80-81 ℃, the temperature at the bottom of the tower is 92-94 ℃, the reflux ratio is 7-7.2, and the pressure at the top of the tower is 0.04-0.05 MPa.
9. The processing method according to any one of claims 3 to 8,
the hydrogenation catalyst in the hydrogenation reactor is FHJ-2 catalyst.
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