CN114540080B - Multi-raw-material n-hexane production device and processing method of n-hexane product - Google Patents

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

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CN114540080B
CN114540080B CN202210262729.0A CN202210262729A CN114540080B CN 114540080 B CN114540080 B CN 114540080B CN 202210262729 A CN202210262729 A CN 202210262729A CN 114540080 B CN114540080 B CN 114540080B
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tower
pipe
side line
light component
aromatic
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CN114540080A (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 normal hexane production device with multiple raw materials, which comprises a separation tower, a hydrogenation reactor, a light component removal tower and a heavy component removal 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 tower bottom pipe A and a first tower bottom pipe B are led out from a tower bottom discharge port of the separation tower, and the first tower bottom pipe B and the first side line pipe A are both communicated with a feed inlet of the hydrogenation reactor; the bottom discharge port of the hydrogenation reactor is communicated with the feed port of the light component removal tower 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 light component removal tower, and a bottom discharge port of the light component removal tower is communicated with a feed port of the heavy component removal tower; and a fourth tower top discharging pipe A and a fourth tower top discharging 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 discharging hole of the weight removing tower. The application also discloses a processing method of the n-hexane product. By using the method, the non-aromatic component oil or the C5-C6 component oil can be used as a raw material, the C6 component is collected, and different n-hexane products can be produced.

Description

Multi-raw-material n-hexane production device and processing method of n-hexane product
Technical Field
The invention relates to a multi-raw-material n-hexane production device and a processing method of an n-hexane product.
Background
At present, non-aromatic component 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 the C5-C6 component oil in the middle of the light naphtha product produced by the hydrogenation cracking device and the topped oil product produced by the reforming device in the refining enterprise is separated by normal component and heterogeneous component, the normal component oil is used as the raw material of the ethylene device, the heterogeneous oil is used as the gasoline blending component, and the added value of the product is not high.
Under the background that chemical products tend to be high-end and increasingly prevail at present, the light component byproducts of the refining device are directly used for blending gasoline or serve as ethylene materials and other conventional product forms to be sold in a factory, so that the improvement of the overall economic benefit of a refinery and the promotion of the high-end development strategy of the products are not facilitated.
Disclosure of Invention
In order to improve the added value of products 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 removal tower and a heavy removal tower, wherein a raw material inlet is arranged on the side wall of the separation tower, two first side line pipes are led out from a first side line discharge hole on 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, wherein the first side line pipe B is communicated with a non-aromatic and gasoline pool, the first side line discharge hole is positioned on the upper side of the raw material inlet, and a first tower top discharge pipe at the top of the separation tower is communicated with the non-aromatic and gasoline pool;
two first tower bottom pipes are led out from a first tower bottom discharge port at the tower bottom of the separation tower, the two first tower bottom pipes are a first tower bottom pipe A and a first tower bottom pipe B 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 a second feeding port at the tower top of the hydrogenation reactor through a feeding pump, a second tower bottom discharging port at the tower bottom of the hydrogenation reactor is communicated with a separating tank, and a liquid discharging port at the bottom of the separating tank is communicated with a third feeding port on the side wall of the light component removal tower;
two third side line pipes are led out from a third side line discharge port on the side wall of the light removal 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 a solvent tank, the third side line pipe B is communicated with a non-aromatic blending gasoline pool, the third side line discharge port is positioned at the upper side of a raw material inlet, a third tower top discharge pipe on the top of the light removal tower is communicated with the non-aromatic blending gasoline pool, and a third tower bottom discharge port on the bottom of the light removal tower is communicated with a fourth feed port on the side wall of the heavy removal tower;
two fourth tower top discharging pipes are led out from a fourth tower top discharging hole of the tower top of the heavy removal tower, the two fourth tower top discharging pipes are a fourth tower top discharging pipe A and a fourth tower top discharging pipe B respectively, wherein 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 medicine-grade additive tank, two fourth tower bottom pipes are led out from a fourth tower bottom discharging hole of the tower bottom of the heavy removal tower, the two fourth tower bottom pipes are a fourth tower bottom pipe A and a fourth tower bottom pipe B respectively, 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 and gasoline pool.
The n-hexane production device can adopt non-aromatic component oil or C5-C6 component oil as raw materials, and collect C6 components in the raw materials so as to produce n-hexane products of different varieties. When the non-aromatic component oil is used as a raw material, a C6 crude product is collected from a first side line discharge port of the separation tower, when the C5-C6 component oil is used as the raw material, the C6 crude product is collected from the bottom of the separation tower, then the C6 crude product is subjected to hydrotreatment and then sequentially subjected to twice separation by a light component removal tower and a heavy component removal tower, and then a normal hexane product is collected from the top of the heavy component removal tower, wherein when the non-aromatic component oil is used as the raw material, more than 80.5wt% of normal hexane is collected, and when the C5-C6 component oil is used as the raw material, 99.5wt% of normal hexane is collected. The n-hexane production device can adapt to different raw materials and produce corresponding n-hexane products, and improves the added value of products 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 can be 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 component oil, the theoretical plate number of the separating 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 trays was counted from bottom to top. Through the process, the raw materials required by the n-hexane reactor can be fully refined, and the yield of the target product is improved.
The processing method comprises the steps of separating the raw materials through a separation tower to obtain a C6 crude product, then hydrogenating the C6 crude product through a hydrogenation reactor to obtain a saturated material, separating the saturated material to obtain crude n-hexane, removing light components from the crude n-hexane through a light component removal tower, introducing the bottom material of the light component removal tower into a heavy component removal tower, and collecting the n-hexane from the top of the heavy component removal tower.
By the processing method, reasonable configuration of main products and byproducts of the device can be realized, and analysis results and product yields of all components are ensured. Benzene and phenyl in the C6 crude product are saturated by hydrogenation to form naphthene, namely, the debenzolization reaction is carried out. When non-aromatic component oil is used as the raw material, the yield of the normal hexane product is more than or equal to 50 percent relative to the normal hexane content in the raw material. When the C5-C6 component oil is used as the raw material, the energy yield of the n-hexane product is more than or equal to 93 percent relative to the n-hexane content in the raw material.
Specifically, when the feedstock is a non-aromatic component oil, the processing method comprises the steps of:
separating non-aromatic component oil by a separating tower, wherein a first tower top light component A of the separating tower enters a non-aromatic blending gasoline pool by a first tower top discharging pipe, a C6 crude product is collected by a first side line pipe A, and a first tower bottom oil A of the separating tower enters the non-aromatic blending gasoline pool by a first tower bottom pipe A;
(1.2) mixing the C6 crude product with hydrogen to form a hydrogenation raw material in a gas-liquid mixed phase state, enabling the hydrogenation raw material to enter a hydrogenation reactor for carrying out aromatic saturation reaction to obtain a saturated material, separating the saturated material by a separating tank to obtain crude hydrogen and crude n-hexane in a liquid phase, wherein the crude hydrogen is recycled after passing through a recycle hydrogen compressor;
the crude n-hexane enters a light component removal tower through a third feeding port for separation, a third tower top light component A of the light component removal tower enters a non-aromatic blending gasoline pool through a third tower top discharging pipe, vegetable oil is extracted from a third side pipe A of the light component removal tower to extract solvent oil, and a third tower bottom material A of the light component removal tower enters a heavy component removal tower through a fourth feeding port for separation;
the light component A at the top of the fourth tower of the de-weight tower is extracted by a discharging pipe A at the top of the fourth tower to be more than 80.5 weight percent of normal hexane, and the bottom material of the de-weight tower is extracted as petroleum ether; more than 80.5wt% 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 C5-C6 component oil by a separating tower, wherein a first tower top light component B of the separating tower enters a non-aromatic blending gasoline pool through a first tower top discharging pipe, a first side line light component B is collected by a first side line pipe B and enters the non-aromatic blending gasoline pool, and a first tower bottom oil B of the separating tower is used as a C6 crude product;
(2.2) mixing the C6 crude product with hydrogen to form a hydrogenation raw material in a gas-liquid mixed phase state, enabling the hydrogenation raw material to enter a hydrogenation reactor for carrying out aromatic saturation reaction to obtain a saturated material, separating the saturated material by a separating tank to obtain crude hydrogen and crude n-hexane in a liquid phase, wherein the crude hydrogen is recycled after passing through a recycle hydrogen compressor;
(2.3) crude normal hexane enters a light component removal tower through a third feeding port to be separated, a third tower top light component B of the light component removal tower enters a non-aromatic blending gasoline pool through a third tower top discharging pipe, a third side line pipe B of the light component removal 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 light component removal tower enters a heavy component removal tower through a fourth feeding port to be separated;
the light component B at the fourth tower top of the de-weight tower is extracted by the discharging pipe B at the fourth tower top, 99.5 weight percent of normal hexane is extracted, the tower bottom material of the de-weight tower enters a non-aromatic blending gasoline pool, and 99.5 weight percent of normal hexane can be used as a medical grade additive.
In this application, utilize above-mentioned normal hexane apparatus for producing, adopt different raw materials in order to produce normal hexane of different piece qualities, owing to adopted same set of device, can reduce the investment of equipment. The non-aromatic component oil or the C5-C6 component oil which is rich in the C6 component is used as the raw material, so that the added value of the product of the non-aromatic component oil or the C5-C6 component oil can be effectively improved, wherein the non-aromatic component 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 heterogeneous components from at least one of topped oil produced by a pre-hydrogenation fractionating tower of the continuous reforming device and light naphtha produced by a naphtha fractionating tower top of a hydrocracking device. The C5-C6 component oil is normal oil obtained by separating normal isomerism components from topped oil produced by a pre-hydrogenation fractionating tower of a continuous reforming device, or normal oil obtained by separating normal isomerism components from light naphtha produced by a naphtha fractionating tower top of a hydrocracking device, or mixed oil of the two normal oils.
By using non-aromatic component oil or C5-C6 component oil as processing raw materials, high-value n-hexane products with different purities can be refined, and byproducts can be reasonably utilized as gasoline blend oil and ethylene blend raw materials. When the non-aromatic component oil is used as the 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 plus 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 raw materials, in the step (1.1), the operation process parameters of the separation tower are as follows: the temperature of the tower top is 81-83 ℃, the temperature of the tower bottom is 156-165 ℃, the reflux ratio is 1.70-1.90, and the pressure of the tower top 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 tower top is 60-62 ℃, the temperature of the tower bottom is 96-98 ℃, the reflux ratio is 0.65-0.68, and the pressure of the tower top is 0.130-0.135 MPa.
Through the adjustment within a certain interval range, the allowance can be reserved for the operation parameters of the device under the condition of ensuring the qualification of the main product, and the anti-fluctuation capability is improved.
Further, because the raw materials are different, the specific components contained in the C6 crude product are different, in order to be better suitable for the C6 crude product collected by different raw materials, in the step (1.2), the operation technological 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 operation 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 excavated by adjusting the reaction temperature and the reaction pressure, and meanwhile, the yield of target products and the maximization of device benefits are ensured.
Specifically, in the step (1.3), the operation process parameters of the light component removal tower are as follows: the temperature of the tower top is 70-72 ℃, the temperature of the tower bottom is 98-99 ℃, the reflux ratio is 1.9-2.1, and the pressure of the tower top 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 of the tower top is 77-79 ℃, the temperature of the tower bottom is 90-93 ℃, the reflux ratio is 1.9-2.1, and the pressure of the tower top is 0.04-0.05 MPa.
By maintaining the reaction parameters, the separation effect of the rectifying tower can be ensured, and the maximization of the product yield can be ensured.
Specifically, in the step (1.3), the operation process parameters of the heavy-duty removal tower are as follows: the temperature of the tower top is 80-81 ℃, the temperature of the tower bottom is 108-110 ℃, the reflux ratio is 6.2-6.8, and the pressure of the tower top is 0.04-0.05;
in the step (2.3), the operation process parameters of the heavy-duty removal tower are as follows: the temperature of the tower top is 80-81 ℃, the temperature of the tower bottom is 92-94, the reflux ratio is 7-7.2, and the pressure of the tower top is 0.04-0.05.
By maintaining the reaction parameters, the separation effect of the rectifying tower can be ensured, the maximization of the product yield is ensured, and a certain fluctuation interval is allowed.
In the present application, the reflux ratio is a ratio of the reflux amount to the feed amount.
Specifically, in order to make hydrogenation proceed smoothly, the hydrogenation catalyst in the hydrogenation reactor is FHJ-2 catalyst. The catalyst can ensure the removal efficiency of benzene in raw materials and ensure the operation time of a single overhaul period of the device.
Drawings
FIG. 1 is a schematic diagram of an embodiment of the present invention.
Detailed Description
A multi-raw-material n-hexane production apparatus comprises a separation column 10, a hydrogenation reactor 20, a light component removal column 30 and a heavy component removal column 40, wherein a raw material inlet 11 is arranged on the side wall of the separation column 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 arranged on the first feeding pipe 111, and a second feeding valve 114 is arranged on the second feeding pipe 113. Two first side line 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 line pipes are a first side line pipe A131 and a first side line pipe B133 respectively, wherein the first side line pipe B is communicated with a non-aromatic gasoline pool, the first side line discharge port is positioned on 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 reflux tank 121, the first reflux tank 121 is communicated with the separation tower through a first reflux pipe 122, and a first tower top discharge pipe 123 is further connected to the bottom of the first reflux tank 121 and is communicated with the non-aromatic 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.
The first bottom discharge port 14 at the bottom of the separation column 10 leads out two first bottom pipes, namely a first bottom pipe A141 and a first bottom pipe B143, wherein the first bottom pipe A is communicated with a non-aromatic blend gasoline pool. The first bottom line B and the first side line a are both in communication with the inlet of the feed pump 61. A first bottom switching valve a142 is attached to the first bottom pipe a141, and a first bottom switching valve B144 is attached to the first bottom pipe B143.
In the embodiment, the theoretical plate number of the separation tower is 100, the feeding position is 13 th, and the first side line discharge hole is positioned at 65 th. The number of the tower plates of the separation tower is counted from bottom to top.
The outlet pipe 211 of the feed pump is sequentially communicated with the second feed port 21 at the top of the hydrogenation reactor 20 after passing through the refrigerant passage of the heat exchanger 62 and the heater 64, and the outlet pipe 211 is connected with a hydrogenation pipe 212, 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 transfer 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 is sequentially communicated with the tank inlet 51 of the separation tank 50 after passing through the heat medium channel of the heat exchanger 62 and the cooler 63, the top of the separation tank is connected with a hydrogen discharge pipe 52, and the liquid outlet 53 at the bottom of the separation tank is communicated with the third feed port 31 on the side wall of the light component removal tower 30.
The third side line discharge port 33 on the side wall of the light component removal tower 30 is led out of two third side line pipes, 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 gasoline pool, and the third side line discharge port is positioned on the upper side of the raw material inlet. The third side line pipe a331 is provided with a third side line switching valve a332, and the third side line pipe B333 is provided with a third side line switching valve B334.
The third top of the tower discharge gate 32 of the light component removal tower 30 is connected with a third reflux tank 321, the third reflux tank 321 is communicated with the light component removal tower through a third reflux pipe 322, the bottom of the third reflux tank 321 is also connected with a third top of the tower discharge pipe 323, and the first top of the tower discharge pipe is communicated with a non-aromatic gasoline pool. The third bottom discharge port 34 at the bottom of the light component removal tower is communicated with a fourth feed port 41 on the side wall of the heavy component removal tower 40.
The fourth tower top discharge port 42 of the tower top of the weight removing tower 40 is connected with a fourth reflux tank 421, the fourth reflux tank 421 is communicated with the weight removing tower through a fourth reflux pipe 422, two fourth tower top discharge pipes are led out from the bottom of the fourth reflux tank 421, the two fourth tower top discharge pipes are a fourth tower top discharge pipe A424 and a fourth tower top discharge pipe B426 respectively, wherein the fourth tower top discharge pipe A is communicated with the food grade additive tank, and the fourth tower top discharge pipe B is communicated with the medical grade additive tank. A fourth overhead switching valve a425 is attached to the fourth overhead discharge pipe a, and a fourth overhead switching valve B427 is attached to the fourth overhead discharge pipe B.
The fourth bottom discharge port 43 at the bottom of the weight removing tower 40 is led out of two fourth bottom pipes, which are a fourth bottom pipe A431 and a fourth bottom pipe B433 respectively, wherein the fourth bottom pipe A is communicated with a petroleum ether tank, and the fourth bottom pipe B is communicated with a non-aromatic blending gasoline pool. A fourth column bottom switching valve a432 is attached to the fourth column bottom pipe a431, and a fourth column bottom switching valve B434 is attached to the fourth column bottom pipe B433.
The following describes the processing method of the n-hexane product.
The following first describes a processing method for producing n-hexane using non-aromatic component oil as a raw material, the non-aromatic component oil being produced by an extraction unit of a continuous reforming apparatus, the processing method being produced by using the above-described multi-raw-material n-hexane production apparatus, and specifically comprising the steps of:
(1.1) the first feed valve 112 was opened, the second feed valve 114 was closed, and the non-aromatic component oil 911 was fed into the separation column through the first feed pipe 111 to be separated.
The top gas of the separation tower enters the first reflux tank 121 after being condensed, part of condensate returns to the separation tower, part of condensate becomes a first top light component A920, and the first top light component A920 enters the non-aromatic and gasoline pool through the first top discharging pipe 123.
And closing the first side line switching valve B134, opening the first side line switching valve A132, and collecting the C6 crude product through the first side line discharge port 13. And closing the first tower bottom switching valve B144, and opening the first tower bottom switching valve A142 to enable the first tower bottom oil A940 of the separation tower to enter the non-aromatic blend gasoline pool through the first tower bottom pipe A.
(1.2) mixing the C6 crude product with hydrogen to form a gas-liquid mixed phase hydrogenation raw material, 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 entering a hydrogenation reactor 20 through a second feed port 21 for hydrogenation reaction, carrying out aromatic hydrocarbon saturation reaction on benzene in the hydrogenation reactor to obtain saturated material, discharging the saturated material through a second tower bottom discharge port 22, cooling the saturated material by the heat exchanger 62 and a cooler 63 in sequence, entering 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 outlet pipe 52, and then recycling the crude hydrogen after adjustment through a circulating hydrogen compressor.
And (1.3) crude n-hexane enters the light component removing tower 30 through a third feeding port 31 for separation, the tower top gas of the light component removing tower enters a third reflux tank 321 after being condensed, part of condensate returns to the light component removing tower, part of condensate becomes a third tower top light component A, and the third tower top light component A enters a non-aromatic gasoline blending tank. 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 light component removal tower. The third bottom material A of the light component removal tower enters the heavy component removal tower 40 through the fourth feed inlet 41 for separation.
The tower top gas of the heavy-duty removal tower enters a fourth reflux tank 421 after being condensed, part of condensate returns to the heavy-duty removal tower, a fourth tower top switching valve B427 is closed, a fourth tower top switching valve A425 is opened, part of condensate is extracted from a fourth tower top discharging pipe A to become a fourth tower top light component A981, the fourth tower top light component A981 is used as more than 80.5 weight percent of n-hexane, and more than 80.5 weight percent of n-hexane can be used as a food grade additive.
The fourth bottom switching valve B434 is closed, the fourth bottom switching valve a432 is opened, and the bottom material of the heavy ends removal column is taken out as petroleum ether 991 from the fourth bottom pipe a 431.
In this embodiment, in step (1.1), the operation process parameters of the separation column are: the temperature of the tower top is 81-83 ℃, the temperature of the tower bottom is 158-161 ℃, the reflux ratio is 1.70-1.90, and the pressure of the tower top is 0.13-0.15 MPa. In the step (1.2), the operation 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 of the tower top is 70-72 ℃, the temperature of the tower bottom is 98-99 ℃, the reflux ratio is 1.9-2.1, and the pressure of the tower top is 0.04-0.05 MPa. In the step (1.3), the operation process parameters of the heavy-duty removal tower are as follows: the temperature of the tower top is 80-81 ℃, the temperature of the tower bottom is 108-110 ℃, the reflux ratio (the ratio of reflux to feeding) is 6.2-6.8, and the pressure of the tower top 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 component oil feedstock and product composition
Figure BDA0003551206420000071
TABLE 2 vegetable oil extraction solvent oil composition
Figure BDA0003551206420000072
Figure BDA0003551206420000081
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In this example, the yield of 86% pure n-hexane was 51.1% and the yield of vegetable oil extraction solvent oil was 44.3% based on n-hexane in the non-aromatic oil, and the total yield of both was 95.4%. In this example, the distillation range of the vegetable oil extraction solvent oil is between 61 and 76 ℃ in the normal pressure distillation analysis, while the light component removal tower designed by the patent is operated at 0.04MPa, the tower top temperature is between 70 and 72 ℃, and the distillation ranges of substances are different under different pressures.
The following describes 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 isomerism components from topped oil produced by a prehydrogenation fractionating tower of a continuous reforming device, and the processing method is produced by using the multi-raw-material normal hexane production device and comprises the following specific steps:
(2.1) the first feed valve 112 was closed, the second feed valve 114 was opened, and the C5-C6 component oil 912 was fed into the separation column via the second feed pipe 113 to be separated.
The top gas of the separation tower enters the first reflux tank 121 after being condensed, part of condensate returns to the separation tower, part of condensate becomes a first top light component B, and the first top light component B enters the non-aromatic blend gasoline pool through the first top discharging pipe 123.
And opening a first side line switching valve B134, closing a first side line switching valve A132, and collecting a first side line light component B930 by a first side line pipe B, wherein the first side line light component B enters a non-aromatic blend gasoline pool, and the first bottom oil B of the separation tower is taken as a C6 crude product.
(2.2) mixing the C6 crude product 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 driving of a hydrogenation raw material feeding pump 61, then entering a hydrogenation reactor 20 through a second feeding port 21 for hydrogenation reaction, carrying out aromatic hydrocarbon saturation reaction on benzene in the hydrogenation reactor to obtain saturated materials, discharging the saturated materials through a second tower bottom discharging port 22, cooling the saturated materials by the heat exchanger 62 and a cooler 63 in sequence, then entering a separation tank 50, separating the saturated materials into crude hydrogen 950 and crude n-hexane in the separation tank, discharging the crude hydrogen 950 through a hydrogen discharging pipe 52, and then recycling the crude hydrogen after adjustment through a circulating hydrogen compressor.
And (2.3) crude n-hexane enters the light component removing tower 30 through a third feeding port for separation, the tower top gas of the light component removing tower enters a third reflux tank 321 after being condensed, part of condensate returns to the light component removing tower, part of condensate becomes a third tower top light component B, and the third tower top light component B enters a non-aromatic blending gasoline pool through a third tower top discharging pipe.
And opening a third side line switching valve B334, closing a third side line switching valve A332, and extracting a third side line light component B972 from a third side line pipe B of the light component removal tower, wherein the third side line light component B enters a non-aromatic blend gasoline pool, and a third bottom material B of the light component removal tower enters the heavy component removal tower 40 through a fourth feed inlet 41 for separation.
The tower top gas of the heavy-removal tower enters a fourth reflux tank 421 after being condensed, part of condensate returns to the heavy-removal tower, a fourth tower top switching valve B427 is opened, a fourth tower top switching valve A425 is closed, part of condensate is extracted from a fourth tower top discharging pipe B to become a fourth tower top light component B982, the fourth tower top light component B982 is used as 99.5 weight percent of normal hexane, and 99.5 weight percent of normal hexane can be used as a pharmaceutical grade additive.
And opening a fourth tower bottom switching valve B434, closing a fourth tower bottom switching valve A432, and enabling the bottom materials of the heavy-removal tower to enter a non-aromatic gasoline pool through a fourth tower bottom pipe B.
In this embodiment, in step (2.1), the operation process parameters of the separation column are: the temperature of the tower top is 60-62 ℃, the temperature of the tower bottom is 96-98 ℃, the reflux ratio is 0.65-0.68, and the pressure of the tower top is 0.130-0.135 MPa. In the step (2.2), the operation 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 of the tower top is 77-79 ℃, the temperature of the tower bottom is 90-93 ℃, the reflux ratio is 1.9-2.1, and the pressure of the tower top is 0.04-0.05 MPa. In the step (2.3), the operation process parameters of the heavy-duty removal tower are as follows: the temperature of the tower top is 80-81 ℃, the temperature of the tower bottom is 92-94 ℃, the reflux ratio is 7-7.2, and the pressure of the tower top 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 oil raw Material and product composition
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 will be appreciated that in other embodiments, the C5-C6 component oil may also be normal oil obtained after separation of normal components of light naphtha produced at the top of a naphtha fractionating tower of a hydrocracking unit, or a mixture of normal oil obtained after separation of normal components of topped oil produced at a pre-hydrogenation fractionating tower of a continuous reforming unit, and normal oil obtained after separation of normal components of light naphtha produced at the top of a naphtha fractionating tower of a hydrocracking unit.

Claims (8)

1. A processing method of n-hexane product is characterized in that non-aromatic component oil or C5-C6 component oil is adopted as a raw material, the raw material is separated by a separation tower to obtain a C6 crude product, then the C6 crude product is hydrogenated by a hydrogenation reactor to obtain saturated material, the saturated material is separated to obtain crude n-hexane, the crude n-hexane is subjected to light component removal by a light component removal tower, the bottom material of the light component removal tower enters a heavy component removal tower, and n-hexane is collected from the top of the heavy component removal tower;
when the raw material is non-aromatic component oil, the processing method comprises the following steps:
(1.1) separating the non-aromatic component oil by a separating tower, wherein a first tower top light component A of the separating tower enters the non-aromatic component oil by a first tower top discharging pipe
The method comprises the steps that C6 crude products are collected by a first side line pipe A, and first bottom oil A of a separation tower enters a non-aromatic blending gasoline pool through the first bottom line A;
(1.2) mixing the C6 crude product with hydrogen to form a hydrogenation raw material in a gas-liquid mixed phase state, enabling the hydrogenation raw material to enter a hydrogenation reactor for carrying out aromatic saturation reaction to obtain a saturated material, separating the saturated material by a separating tank to obtain crude hydrogen and crude n-hexane in a liquid phase, wherein the crude hydrogen is recycled after passing through a recycle hydrogen compressor;
(1.3) crude n-hexane enters a light component removal tower through a third feeding port to be separated, a third tower top light component A of the light component removal tower enters a non-aromatic blending gasoline pool through a third tower top discharging pipe, and vegetable oil extraction solvent oil is extracted by a third side pipe A of the light component removal tower; the third bottom material A of the light component removal tower enters the heavy component removal tower through a fourth feed inlet for separation; the light component A at the fourth tower top of the heavy removal tower is extracted by a fourth tower top discharging pipe A to be more than 80.5 weight percent of normal hexane which is used as food and additive, and the bottom material of the heavy removal 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 C5-C6 component oil by a separating tower, wherein a first tower top light component B of the separating tower enters a non-aromatic blending gasoline pool through a first tower top discharging pipe, a first side line light component B is collected by a first side line pipe B and enters the non-aromatic blending gasoline pool, and a first tower bottom oil B of the separating tower is used as a C6 crude product;
(2.2) mixing the C6 crude product with hydrogen to form a hydrogenation raw material in a gas-liquid mixed phase state, enabling the hydrogenation raw material to enter a hydrogenation reactor for carrying out aromatic saturation reaction to obtain a saturated material, separating the saturated material by a separating tank to obtain crude hydrogen and crude n-hexane in a liquid phase, wherein the crude hydrogen is recycled after passing through a recycle hydrogen compressor;
(2.3) crude normal hexane enters a light component removal tower through a third feeding port to be separated, a third tower top light component B of the light component removal tower enters a non-aromatic blending gasoline pool through a third tower top discharging pipe, a third side line pipe B of the light component removal 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 light component removal tower enters a heavy component removal tower through a fourth feeding port to be separated; the light component B at the top of the fourth tower of the heavy removal tower is used as a pharmaceutical grade additive by extracting 99.5 weight percent of normal hexane through a discharging pipe B at the top of the fourth tower; the bottom material of the heavy-removal tower enters a non-aromatic blending gasoline pool.
2. The method according to claim 1, wherein,
in the step (1.1), the operation process parameters of the separation tower are as follows: the temperature of the tower top is 81-83 ℃, the temperature of the tower bottom is 156-165 ℃, the reflux ratio is 1.70-1.90, and the pressure of the tower top 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 tower top is 60-62 ℃, the temperature of the tower bottom is 96-98 ℃, the reflux ratio is 0.65-0.68, and the pressure of the tower top is 0.130-0.135 MPa.
3. The method according to claim 1, wherein,
in the step (1.2), the operation 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 operation 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.
4. The method according to claim 1, wherein,
in the step (1.3), the operation process parameters of the light component removal tower are as follows: the temperature of the tower top is 70-72 ℃, the temperature of the tower bottom is 98-99 ℃, the reflux ratio is 1.9-2.1, and the pressure of the tower top 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 of the tower top is 77-79 ℃, the temperature of the tower bottom is 90-93 ℃, the reflux ratio is 1.9-2.1, and the pressure of the tower top is 0.04-0.05 MPa.
5. The method according to claim 1, wherein,
in the step (1.3), the operation process parameters of the heavy-duty removal tower are as follows: the temperature of the tower top is 80-81 ℃, the temperature of the tower bottom is 108-110 ℃, the reflux ratio is 6.2-6.8, and the pressure of the tower top is 0.04-0.05 MPa;
in the step (2.3), the operation process parameters of the heavy-duty removal tower are as follows: the temperature of the tower top is 80-81 ℃, the temperature of the tower bottom is 92-94 ℃, the reflux ratio is 7-7.2, and the pressure of the tower top is 0.04-0.05 MPa.
6. The method according to any one of claim 1 to 5, wherein,
the hydrogenation catalyst in the hydrogenation reactor is FHJ-2 catalyst.
7. The n-hexane production device of multiple raw materials for the processing method according to any one of claims 1 to 6, which is characterized by comprising a separation tower, a hydrogenation reactor, a light component removal tower and a heavy component removal tower, wherein a raw material inlet is arranged on the side wall of the separation tower, two first side line pipes are led out from a first side line discharge hole on 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, wherein the first side line pipe B is communicated with a non-aromatic blend 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 top of the separation tower is communicated with the non-aromatic blend gasoline pool;
two first tower bottom pipes are led out from a first tower bottom discharge port at the tower bottom of the separation tower, the two first tower bottom pipes are a first tower bottom pipe A and a first tower bottom pipe B 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 a second feeding port at the tower top of the hydrogenation reactor through a feeding pump, a second tower bottom discharging port at the tower bottom of the hydrogenation reactor is communicated with a separating tank, and a liquid discharging port at the bottom of the separating tank is communicated with a third feeding port on the side wall of the light component removal tower;
two third side line pipes are led out from a third side line discharge port on the side wall of the light removal 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 a solvent tank, the third side line pipe B is communicated with a non-aromatic blending gasoline pool, the third side line discharge port is positioned at the upper side of a raw material inlet, a third tower top discharge pipe on the top of the light removal tower is communicated with the non-aromatic blending gasoline pool, and a third tower bottom discharge port on the bottom of the light removal tower is communicated with a fourth feed port on the side wall of the heavy removal tower;
two fourth tower top discharging pipes are led out from a fourth tower top discharging hole of the tower top of the heavy removal tower, the two fourth tower top discharging pipes are a fourth tower top discharging pipe A and a fourth tower top discharging pipe B respectively, wherein 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 medicine-grade additive tank, two fourth tower bottom pipes are led out from a fourth tower bottom discharging hole of the tower bottom of the heavy removal tower, the two fourth tower bottom pipes are a fourth tower bottom pipe A and a fourth tower bottom pipe B respectively, 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 and gasoline pool.
8. The n-hexane production apparatus according to claim 7, wherein the theoretical plate number of the separation column is 80 to 110, the feeding position is 10 to 20, and the first side discharge port is 50 to 70.
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