Device for producing gasoline blending component by taking isopentane as raw material

Abstract

The utility model discloses a device for producing a gasoline blending component by taking isopentane as a raw material. The device comprises a heating furnace (10), a dehydrogenation reactor (16), a stabilization tower (17) and an etherification reactor (18), an isopentane feeding pipeline (1) is connected with an inlet of the heating furnace (10), an outlet of the heating furnace (10) is connected with the dehydrogenation reactor (16) through a dehydrogenation reactor feeding pipeline (8), a hydrogen feeding pipeline (2) is connected to the dehydrogenation reactor (16), a product of the dehydrogenation reactor (16) is connected to the stabilization tower (17) through a dehydrogenation product pipeline (3), and the etherification reactor (18) is connected to the stabilization tower (17). A top outlet of the stabilizing tower is connected with a sending-out area of a stabilizing tower top light component pipeline (6), materials at a bottom outlet of the stabilizing tower are connected with an inlet of the etherification reactor through a stabilizing tower bottom heavy component pipeline (4), an alcohol feeding pipeline (5) is connected to the inlet of the etherification reactor, and an outlet of the etherification reactor is connected with an etherification reaction product pipeline (7). By using the device, the defects of high vapor pressure and low density when the raw material isopentane is used as a gasoline blending component can be effectively improved, and the octane number is increased.

Description

TECHNICAL FIELD

[0001] The utility model belongs to the technical field of petroleum chemical industry relates to a kind of with isopentane as raw material production compared with raw material isopentane The device of the gasoline blending component with lower vapor pressure and higher density. BACKGROUND

[0002] Chemical type refinery, especially large-scale production of paraxylene (PX) project, usually processes wax oil and diesel oil fraction through hydrocracking process to produce heavy naphtha with high conversion rate as raw material for producing aromatic hydrocarbon; this process produces a large amount of light naphtha, plus pentane oil and reforming pre-hydrogenation overhead oil produced by reforming unit, the amount of light naphtha in the entire project will be very large, and subsequent processing and treatment will become a problem. These light naphthas are mainly C5 fraction, which includes isopentane and n-pentane, and isopentane column is usually provided to separate isopentane and n-pentane. N-pentane is usually used as ethylene raw material; isopentane has low density, high vapor pressure and high octane number, and is often used to blend gasoline, and is not suitable as ethylene material.

[0003] At present, refinery isopentane is usually directly used as gasoline blending component, and isopentane material is not further processed before being used as gasoline blending component.

[0004] CN106365947A provides a process method for producing diene and high-octane gasoline component by combining catalytic dehydrogenation, oxidative dehydrogenation and etherification with refinery overhead oil as raw material. The utility model is different from the process provided by the patent in raw material, and the utility model does not produce diene, and the etherification process does not provide alcohol recovery facility.

[0005] CN110437873A provides a process combination for producing etherification gasoline, aromatization oil and propylene by combining catalytic dehydrogenation, etherification and aromatization with reforming overhead oil as raw material, while producing hydrogen as by-product. The utility model is different from the process provided by the patent in raw material, and the utility model product is only one kind, and the etherification process does not provide alcohol recovery facility.

[0006] CN1198431A relates to a process for etherification of tertiary olefins in C5 and above hydrocarbon raw material. It utilizes the feature that light hydrocarbon can form azeotrope with C4 and below alcohol, so that the remaining methanol in the reaction forms azeotrope with C5, and circulates between the reactor and azeotropic distillation column or catalytic distillation column, thereby eliminating the methanol recovery system. The etherification process of the utility model does not provide alcohol recovery facility, and the principle is different from the invention. The utility model controls the reaction depth, so that C5 olefins are excessive and alcohol is insufficient, so that the etherification reaction only needs one reactor. UTILITY MODEL CONTENT

[0007] The utility model discloses a device for producing higher quality gasoline blending component with isopentane as raw material to solve the problem of high vapor pressure and low density when isopentane is directly used as gasoline blending component.

[0008] To achieve the above object, the utility model provides the following technical scheme:

[0009] A device for producing gasoline blending component with isopentane as raw material, characterized in that the device comprises a feed heating furnace, a dehydrogenation reactor, a stabilizing tower and an etherification reactor; an isopentane feed pipeline is connected to the inlet of the heating furnace; the outlet of the heating furnace is connected to the dehydrogenation reactor through a dehydrogenation reactor feed pipeline; a hydrogen feed pipeline is directly connected to the dehydrogenation reactor or is connected to the dehydrogenation reactor after merging with the dehydrogenation reactor feed pipeline; the dehydrogenation reactor is connected to the stabilizing tower through a dehydrogenation product pipeline; the top outlet of the stabilizing tower is connected to a stabilizing tower top light component pipeline; the bottom outlet of the stabilizing tower is connected to the inlet of the etherification reactor through a stabilizing tower bottom heavy component pipeline; an alcohol feed pipeline is directly connected to the inlet of the etherification reactor or is connected to the inlet of the etherification reactor after merging with the stabilizing tower bottom heavy component pipeline; and the outlet of the etherification reactor is connected to an etherification reaction product pipeline.

[0010] Preferably, the isopentane feed pipeline is provided with a raw material heater or a raw material heat exchanger.

[0011] Preferably, the isopentane feed pipeline is connected to the inlet of the heating furnace through a raw material pump.

[0012] Preferably, the dehydrogenation product pipeline, the stabilizing tower top light component pipeline, the stabilizing tower bottom heavy component pipeline and the etherification reaction product pipeline are all provided with heat exchangers.

[0013] Preferably, the hydrogen feed pipeline merges with the dehydrogenation reactor feed pipeline before being connected to the dehydrogenation reactor, and the alcohol feed pipeline merges with the stabilizing tower bottom heavy component pipeline before being connected to the inlet of the etherification reactor.

[0014] Preferably, the dehydrogenation reactor is a fixed bed reactor, a moving bed reactor or a fluidized bed reactor.

[0015] Preferably, the etherification reactor is one or a combination of a fixed bed reactor, an expanded bed reactor and a catalytic distillation reactor.

[0016] Preferably, no alcohol recovery unit is arranged after the etherification reactor.

[0017] Compared with the prior art, the utility model has the following advantages:

[0018] 1) This invention uses a single raw material. After dehydrogenation of isopentane, the product is stabilized to remove light components, and the heavy components at the bottom of the stabilizer are all sent to the etherification reactor for reaction. Compared with other etherification-related technologies, this invention does not have a methanol (or ethanol) recovery unit after etherification. The etherified product does not require any other subsequent processing. After heat exchange and cooling, it can be used as a finished product in gasoline blending production.

[0019] 2) The product of this invention after reaction is a mixture of isopentane, isopentenene, ethers and a small amount of alcohols, and is not intended to produce ether monomers. The product has a lower vapor pressure, higher density and octane number than the raw material isopentane, and is a higher quality gasoline blending component.

[0020] The present invention will be further described in detail below with reference to the accompanying drawings and specific embodiments, but this does not limit the scope of the present invention. Attached Figure Description

[0021] Figure 1 This is a schematic diagram of an apparatus for producing gasoline blending components using isopentane as a raw material, according to this utility model.

[0022] The reference numerals in the figure are:

[0023] 1. Isopentane feed line; 2. Hydrogen feed line; 3. Dehydrogenation product line; 4. Stabilizer bottom heavy component line; 5. Alcohol feed line; 6. Stabilizer light component line; 7. Etherification reaction product line; 8. Dehydrogenation reactor feed line; 9. Feed pump; 10. Heating furnace; 11. Dehydrogenation reaction product heat exchanger; 12. Stabilizer top heat exchanger; 13. Stabilizer bottom heat exchanger; 14. Etherification reaction product heat exchanger; 15. Isopentane feed heat exchanger; 16. Dehydrogenation reactor; 17. Stabilizer; 18. Etherification reactor. Detailed Implementation

[0024] like Figure 1 As shown, an apparatus for producing gasoline blending components using isopentane as a raw material includes a heater 10, a dehydrogenation reactor 16, a stabilizer tower 17, and an etherification reactor 18. An isopentane feed line 1 is sequentially connected to a feed pump 9, a feed heat exchanger 15, and the inlet of the heater 10. The outlet of the heater 10 is connected to the dehydrogenation reactor 16 via a feed line 8. A hydrogen feed line 2 is connected to the dehydrogenation reactor 16. The product from the dehydrogenation reactor 16 is connected to the stabilizer tower 17 via a dehydrogenation product line 3. The top outlet of the stabilizer tower 17 is connected to a light component line 6 at the top of the stabilizer tower. The bottom outlet of the stabilizer tower 17 is connected to the inlet of the etherification reactor 18 via a heavy component line 4 at the bottom of the stabilizer tower. An alcohol feed line 5 is connected to the inlet of the etherification reactor 18. The outlet of the etherification reactor 18 is connected to an etherification reaction product line 7.

[0025] The dehydrogenation reactor overhead heat exchanger 11 is arranged on the dehydrogenation product pipeline 3.

[0026] The stabilizer overhead heat exchanger 12 is arranged on the stabilizer overhead heavy component pipeline 6.

[0027] The stabilizer bottom heat exchanger 13 is arranged on the stabilizer bottom heavy component pipeline 4.

[0028] The etherification reactor heat exchanger 14 is arranged on the etherification product pipeline 7.

[0029] The dehydrogenation reactor 16 is usually recommended to be a fixed bed reactor, a moving bed reactor or a fluidized bed reactor.

[0030] The etherification reactor 18 is usually recommended to be one or a combination of a fixed bed reactor, an expanded bed reactor and a catalytic distillation reactor.

[0031] The device for producing gasoline blending components by using isopentane as raw material is simple in operation process.

[0032] 1) The isopentane raw material is heated by the heating furnace 10 after being pressurized and heat-exchanged through the isopentane feeding pipeline 1, then is mixed with hydrogen gas entering through the hydrogen gas feeding pipeline 2, and enters the dehydrogenation reactor 16 to generate a dehydrogenation reaction; the product after the reaction is sent out through the dehydrogenation product pipeline 3, and is heat-exchanged through the dehydrogenation reactor overhead heat exchanger 11 and then sent to the stabilizer 17;

[0033] 2) In the stabilizer 17, the dehydrogenation product rich in olefins from step 1) removes light components, and the light components are sent out of the device through the stabilizer light component pipeline 6; the heavy components rich in olefins at the bottom of the stabilizer 17 are sent out through the stabilizer bottom heavy component pipeline 4, heat-exchanged through the stabilizer bottom heat exchanger 13, mixed with alcohol (methanol and / or ethanol) entering through the alcohol feeding pipeline 5, and then sent to the etherification reactor 18;

[0034] 3) In the etherification reactor 18, the heavy components rich in olefins from the bottom of the stabilizer 17 are mixed with alcohol to generate an etherification reaction, and the reaction product is sent out through the etherification product pipeline 7 and heat-exchanged through the etherification product heat exchanger 14 to be used as a gasoline blending component.

[0035] The isopentane raw material refers to isopentane raw material with an isopentane content of more than 60 wt%, preferably more than 90 wt%.

[0036] The catalytic dehydrogenation catalyst in the catalytic dehydrogenation unit is not particularly limited, and the reactor can be a fixed bed, a moving bed or a fluidized bed reactor.

[0037] The etherification catalyst in the etherification unit is not particularly limited.

[0038] The alcohol refers to methanol and ethanol, or a mixture of both without a limited proportion.

[0039] The etherification reactor used in the etherification unit is not particularly limited in the utility model, and can be one or a combination of a fixed bed, an expanded bed or a catalytic distillation reactor.

[0040] When methanol is used as the raw material in the etherification unit, the etherification product is a mixture of isopentane, methyl tert-pentyl ether and C5 olefins such as 2-methyl-2-butene, 2-methyl-1-butene and 3-methyl-1-butene; the mixture has a density of 0.01-0.1 g / mL higher than that of the raw material isopentane and a steam pressure of 15-45 kPa lower than that of the raw material isopentane.

[0041] When ethanol is used as the raw material in the etherification unit, the etherification product is a mixture of isopentane, tert-pentyl ether and C5 olefins such as 2-methyl-2-butene, 2-methyl-1-butene and 3-methyl-1-butene. The mixture has a density of 0.03-0.12 g / mL higher than that of the raw material isopentane and a steam pressure of 15-45 kPa lower than that of the raw material isopentane.

[0042] Example 1

[0043] The raw material isopentane (purity 99 wt%) is subjected to a dehydrogenation reactor under the conditions of a temperature of 560 DEG C, a pressure of 0.17 MPa, a mass space velocity of isopentane of 2.5 h-1 and a hydrogen / hydrocarbon molar ratio of 1, and the reaction product is subjected to a stabilizer to remove light components. The low heavy components of the stabilizer are mixed with methanol from a tank area under the conditions of an alcohol / olefin molar ratio of 0.95, a space velocity of 1.0 h-1 and a reaction temperature of 60 DEG C, so that etherification reaction occurs, and the reaction product contains 41.3 wt% isopentane, 52.9 wt% methyl tert-pentyl ether, 5.5 wt% pentene and a small amount of methanol. The mixed product has a density of 0.69 g / cm3, an RON of about 98, an olefin content of 6% (by volume), an oxygen content of 8.3 wt% and a steam pressure of 77.7 kPa. -1 -1 3

[0044] Example 2

[0045] The raw material isopentane (purity 99 wt%) is subjected to a dehydrogenation reactor under the conditions of a temperature of 560 DEG C, a pressure of 0.17 MPa, a mass space velocity of isopentane of 2.5 h-1 and a hydrogen / hydrocarbon molar ratio of 1, and the reaction product is subjected to a stabilizer to remove light components. The low heavy components of the stabilizer are mixed with methanol from a tank area under the conditions of an alcohol / olefin molar ratio of 0.95, a space velocity of 1.0 h-1 and a reaction temperature of 60 DEG C, so that etherification reaction occurs, and the reaction product contains 41.3 wt% isopentane, 52.9 wt% methyl tert-pentyl ether, 5.5 wt% pentene and a small amount of methanol. The mixed product has a density of 0.69 g / cm3, an RON of about 98, an olefin content of 6% (by volume), an oxygen content of 8.3 wt% and a steam pressure of 77.7 kPa. -1 -1 ​​​​, the reaction temperature 60℃, the etherification reaction occurs, the reaction product contains 38.6wt% isopentane, 56.2wt% tertiary amyl ether, 5.2wt% pentene and trace ethanol. The mixed product density 0.70g / cm 3 RON about 95.8, olefin 5.7% (volume), oxygen content 7.7wt%, vapor pressure 72.4kPa.

[0046] The device for producing high-quality gasoline blending component by using isopentane as raw material can effectively reduce the vapor pressure of isopentane used as gasoline blending component, increase the density and improve the octane value, so that the material is easier to blend and produce gasoline.

[0047] The preferred embodiments of the patent are described in detail above, but the patent is not limited to the above embodiments, and various changes can be made within the knowledge of those skilled in the art without departing from the purpose of the patent.

Claims

1. An apparatus for producing a gasoline blending component from isopentane, characterized by: The device comprises a heating furnace (10), a dehydrogenation reactor (16), a stabilizing tower (17) and an etherification reactor (18), an isopentane feed pipeline (1) is connected to the inlet of the heating furnace (10), the outlet of the heating furnace (10) is connected to the dehydrogenation reactor (16) through a dehydrogenation reactor feed pipeline (8), a hydrogen feed pipeline (2) is directly connected to the dehydrogenation reactor (16) or is connected to the dehydrogenation reactor (16) after being combined with the dehydrogenation reactor feed pipeline (8), the product of the dehydrogenation reactor (16) is connected to the stabilizing tower (17) through a dehydrogenation product pipeline (3), the top outlet of the stabilizing tower is connected to a stabilizing tower top light component pipeline (6), the bottom outlet of the stabilizing tower is connected to the inlet of the etherification reactor through a stabilizing tower bottom heavy component pipeline (4), an alcohol feed pipeline (5) is directly connected to the inlet of the etherification reactor or is connected to the inlet of the etherification reactor after being combined with the stabilizing tower bottom heavy component pipeline (4), and the outlet of the etherification reactor is connected to an etherification reaction product pipeline (7).

2. A plant for producing a gasoline blending component from isopentane according to claim 1, characterized in that: A raw material heater or a raw material heat exchanger is arranged on the isopentane feed pipeline (1).

3. The apparatus for producing a gasoline blending component from isopentane according to claim 1, characterized by: The isopentane feed pipeline (1) is connected to the inlet of the heating furnace (10) through a raw material pump (9).

4. The apparatus for producing a gasoline blending component from isopentane according to claim 1, characterized by: Heat exchangers are arranged on the dehydrogenation product pipeline (3), the stabilizing tower top light component pipeline (6), the stabilizing tower bottom heavy component pipeline (4) and the etherification reaction product pipeline (7).

5. The apparatus for producing a gasoline blending component from isopentane according to claim 1, characterized by: The dehydrogenation reactor (16) is a fixed bed reactor, a moving bed reactor or a fluidized bed reactor.

6. The apparatus for producing a gasoline blending component from isopentane according to claim 1, characterized by: The etherification reactor (18) is one or a combination of a fixed bed reactor, an expanded bed reactor and a catalytic distillation reactor.

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