Olefin hydrogenation saturation system in pentane oil component

Abstract

The utility model provides an olefin hydrogenation saturation system in pentane oil components. The olefin hydrogenation saturation system comprises a hydrogen inlet pipeline and a pentane oil feeding pipeline, a pentane oil feeding pipeline is connected to a hydrogenation reactor, and a C4 raw material buffer tank, a hydrogenation feeding pump, a start-up heater and a raw material oil heat exchanger are sequentially connected to the pentane oil feeding pipeline; the hydrogen inlet pipeline is connected to the pentane oil feeding pipeline, and the hydrogen inlet pipeline is arranged between the start-up heater and the raw oil heat exchanger; an outlet of the hydrogenation reactor is connected to the deisobutanizer through a hydrogenated product discharging pipeline; a tower bottom outlet of the deisobutanizer is connected to a normal isomerization device through an alkylated oil pipeline; the alkylated oil pipeline is sequentially connected with an alkylated oil separation tower air cooler, an alkylated oil separation tower return tank, a refrigerant circulating pump and a light alkylated oil cooler; the problem that the bromine index in normal and isomeric products exceeds the standard due to the fact that the olefin content in the components of the reformed pentane oil is too high can be solved.

Description

TECHNICAL FIELD

[0001] The utility model belongs to the field of chemical technology, especially olefin hydrogenation saturation system in pentane oil component. BACKGROUND

[0002] At present, pentane oil from reforming is because the olefin content in its component is too high, which leads to the bromine index of normal isomerization product foaming agent exceeding the standard, and cannot reach the qualified standard of factory. CONTENT

[0003] In view of above problem, the purpose of the present application is to provide olefin hydrogenation saturation system in pentane oil component, which can meet the product index requirement, add a hydrogenation reactor in alkylating unit raw material pretreatment unit, after hydrogenation, the product is sent to normal isomerization separation device after hydrogen is removed, and solve the problem that the bromine index of normal isomerization product in pentane oil from reforming is too high because the olefin content in its component is too high.

[0004] In order to achieve part or all of the above purposes or other purposes, the present application provides the following technical scheme: olefin hydrogenation saturation system in pentane oil component, including hydrogen gas inlet pipeline and pentane oil feed pipeline, the pentane oil feed pipeline is connected to the hydrogenation reactor, the pentane oil feed pipeline is sequentially connected to carbon four raw material buffer tank, hydrogenation feed pump, start-up heater and raw material oil heat exchanger, the hydrogen gas inlet pipeline is connected to the pentane oil feed pipeline, the hydrogen gas inlet pipeline is arranged between the start-up heater and the raw material oil heat exchanger, the outlet of the hydrogenation reactor is connected to the deisobutane column through the hydrogenation product discharge pipeline, the hydrogenation product discharge pipeline is connected to the start-up heater, the top outlet of the deisobutane column is connected to the top inlet of the deisobutane column through the top reflux pipeline, the top reflux pipeline is sequentially connected to the top air cooler, the top reflux tank and the top reflux pump, the bottom outlet of the deisobutane column is connected to the normal isomerization device through the alkylated oil pipeline, the alkylated oil pipeline is sequentially connected to the alkylated oil separation column air cooler, the alkylated oil separation column reflux tank, the refrigerant circulating pump and the light alkylated oil cooler.

[0005] Further, the bottom outlet of the deisobutane column is connected to the bottom inlet of the deisobutane column through the bottom reflux pipeline, and the bottom reflux pipeline is connected to the deisobutane column bottom reboiler.

[0006] Further, it further includes condensate pipeline, and the condensate pipeline is sequentially connected to the deisobutane column bottom reboiler and the deisobutane reboiler condensate tank.

[0007] Further, the tank top of the top reflux tank is connected to the fuel gas pipeline network through the non-condensable gas pipeline, and a valve is arranged on the non-condensable gas pipeline.

[0008] Further, a first bypass cross line is arranged on the pentane oil feed line, the first bypass cross line is connected between the front line and the rear line of the hydrogenation feed pump, and a second hydrogenation feed pump is arranged on the first bypass cross line.

[0009] Further, a second bypass cross line is arranged on the alkylate oil line, the second bypass cross line is connected between the front line and the rear line of the refrigerant circulating pump, and an alkylate oil separation tower reflux pump is arranged on the second bypass cross line.

[0010] Further, a valve is arranged on the front line of the overhead air cooler, a valve is arranged on the rear line of the overhead reflux pump, a valve is arranged on the front line of the alkylate oil separation tower air cooler, and a valve is arranged on the rear line of the light alkylate oil cooler.

[0011] Compared with the prior art, the alkylate device of the utility model has the beneficial effects that: the alkylate device can meet the product index requirements, a hydrogenation reactor is newly arranged in the raw material pretreatment unit of the alkylate device, and the product after hydrogenation is sent to the normal and isomer separation device after hydrogen is removed; and the problem that the bromine index in the normal and isomer product exceeds the standard due to the high olefin content in the pentane oil from the reforming is solved. BRIEF DESCRIPTION OF DRAWINGS

[0012] Fig. 1 It is a structural schematic diagram of the utility model;

[0013] Fig. 2 It is a structural schematic diagram of the hydrogenation part;

[0014] Fig. 3 It is a structural schematic diagram of the de-isobutane column part;

[0015] In the drawing: 1, carbon four raw material buffer tank, 2, hydrogenation feed pump, 3, start-up heater, 4, raw oil heat exchanger, 5, hydrogenation reactor, 6, de-isobutane column, 7, overhead air cooler, 8, overhead reflux tank, 9, overhead reflux pump, 10, alkylate oil separation tower air cooler, 11, alkylate oil separation tower reflux tank, 12, refrigerant circulating pump, 13, light alkylate oil cooler, 14, de-isobutane column bottom reboiler, 15, de-isobutane reboiler condensate tank, 16, alkylate oil separation tower reflux pump, 17, second hydrogenation feed pump, 101, pentane oil feed line, 102, hydrogenation product discharge line, 103, overhead reflux line, 104, alkylate oil line, 105, bottom reflux line, 106, condensate line, 107, non-condensable gas line, 108, first bypass cross line, 109, second bypass cross line. DETAILED DESCRIPTION

[0016] In order to make the structure and function of the utility model clearer, the technical scheme in the utility model embodiment will be clearly and completely described below by combining the drawings in the utility model embodiment.

[0017] Referring to the drawings Figs. 1-3 , the olefin hydrogenation saturation system in the pentane oil component includes a hydrogen gas inlet pipeline 100 and a pentane oil feed pipeline 101; the pentane oil feed pipeline 101 is connected to a hydrogenation reactor 5, and a carbon four raw material buffer tank 1, a hydrogenation feed pump 2, a start-up heater 3 and a raw material oil heat exchanger 4 are sequentially connected to the pentane oil feed pipeline 101; the hydrogen gas inlet pipeline 100 is connected to the pentane oil feed pipeline 101, and the hydrogen gas inlet pipeline 100 is arranged between the start-up heater 3 and the raw material oil heat exchanger 4; the outlet of the hydrogenation reactor 5 is connected to a de-isobutane column 6 through a hydrogenation product discharge pipeline 102, and the start-up heater 3 is connected to the hydrogenation product discharge pipeline 102; the overhead outlet of the de-isobutane column 6 is connected to the overhead inlet of the de-isobutane column 6 through an overhead reflux pipeline 103, and a top air cooler 7, an overhead reflux tank 8 and an overhead reflux pump 9 are sequentially connected to the overhead reflux pipeline 103; the bottom outlet of the de-isobutane column 6 is connected to a normal isomerization device through an alkylated oil pipeline 104, and an alkylated oil separation column air cooler 10, an alkylated oil separation column reflux tank 11, a refrigerant circulating pump 12 and a light alkylated oil cooler 13 are sequentially connected to the alkylated oil pipeline 104.

[0018] Based on the above technical scheme, the pentane oil from outside the device is temporarily stored in the carbon four raw material buffer tank 1, and after being pressurized by the hydrogenation feed pump 2, it enters the start-up heater 3 and exchanges heat with the reactor hydrogenation product; the hydrogen gas from outside the device is reduced in pressure and mixed with the pentane oil, and after being heated by the raw material oil heat exchanger 4, the mixed raw material oil enters the hydrogenation reactor 5.

[0019] The catalyst inside the hydrogenation reactor 5 is filled, first with high-efficiency large-prize-chapter inert materials placed at the top layer of the inlet, and then with active graded materials placed on the upper part of the nickel catalyst; the large-prize-chapter void fraction is 55 to 60%, the active graded material void fraction is 48 to 50%, and the three-leaf clover type nickel catalyst void fraction is about 43%.

[0020] The hydrogenation reactor 5 is a fixed-bed catalytic reactor, and the raw material oil and hydrogen gas contact the catalyst in the hydrogenation reactor 5 to occur olefin saturation reaction, and the hydrogenation product exchanges heat with the raw material oil through the start-up heater 3 and then enters the de-isobutane column 6.

[0021] The overhead operating pressure of the de-isobutane column 6 is 0.68 MPag, and the operating temperature is 96.25℃; the de-isobutane column overhead gas phase is condensed and cooled by the de-isobutane column overhead air cooler 7 and then enters the de-isobutane column overhead reflux tank 8, and the non-condensable gas discharged from the top of the de-isobutane column overhead reflux tank 8 is sent to the fuel gas pipeline network; the bottom liquid phase is pressurized by the de-isobutane column overhead reflux pump 9 and then returns to the de-isobutane column 6.

[0022] The de-isobutane column bottom reboiler 14 uses medium pressure steam as a heat source, and the de-isobutane column 6 bottom liquid phase is condensed and cooled by the alkylate oil separation column air cooler 10, enters the alkylate oil separation column reflux tank 11, and is pressurized by the alkylate oil separation column reflux pump 16 or the refrigerant circulating pump 12 before being sent to the normal isomerization device.

[0023] The bottom outlet of the de-isobutane column 6 is connected to the bottom inlet of the de-isobutane column 6 through a bottom reflux pipeline 105, and the de-isobutane column bottom reboiler 14 is connected to the bottom reflux pipeline 105.

[0024] A condensate water pipeline 106 is further included, which is connected to the de-isobutane column bottom reboiler 14 and the de-isobutane reboiler condensate tank 15 in sequence.

[0025] The tank top of the overhead reflux tank 8 is connected to the fuel gas pipeline network through a non-condensable gas pipeline 107, and a valve is arranged on the non-condensable gas pipeline 107.

[0026] A first bypass cross line 108 is arranged on the pentane oil feed pipeline 101, and the first bypass cross line 108 is connected between the front route and the rear route of the hydrogenation feed pump 2, and a second hydrogenation feed pump 17 is arranged on the first bypass cross line 108.

[0027] A second bypass cross line 109 is arranged on the alkylate oil pipeline 104, and the second bypass cross line 109 is connected between the front route and the rear route of the refrigerant circulating pump 12, and an alkylate oil separation column reflux pump 16 is arranged on the second bypass cross line 109.

[0028] A valve is arranged on the front route of the overhead air cooler 7, and a valve is arranged on the rear route of the overhead reflux pump 9; a valve is arranged on the front route of the alkylate oil separation column air cooler 10, and a valve is arranged on the rear route of the light alkylate oil cooler 13.

[0029] The method of the above technical solution for hydrogenating and saturating olefins in the pentane oil component: the pentane oil from the reforming device is mixed with 1500 standard liters of hydrogen to enter the hydrogenation reactor 5 at a feed rate of 60 t / h, the feed temperature is controlled to be 90-130℃, the reactor pressure is 2.3 MPa, and the olefin component in the saturated pentane oil is saturated.

[0030] The carbon five olefin hydrogenation saturation technology is mainly related to converting olefins in the carbon five fraction into saturated hydrocarbons through hydrogenation reaction to improve the stability and safety of the oil product.

[0031] Preferably, two-stage hydrogenation technology is adopted to more effectively hydrogenate the olefins in the C5 fraction; in the first stage, the optimal process conditions are 3 MPa of pressure, 60℃ of reaction temperature, 2 h-1 of space velocity, and 300:1 of hydrogen / oil volume ratio; in the second stage, the optimal process conditions are 3 MPa of pressure, 160℃ of reaction temperature, 2 h-1 of space velocity, and 200:1 of hydrogen / oil volume ratio; this process can reduce the iodine value of the C5 fraction from 16.3 g(I) / 100 g to 0.1 g(I) / 100 g, and the saturation degree of di-olefins almost reaches 100%, and the bromine value is reduced from 81.4 g(Br) / 100 g to 2.5 g(Br) / 100 g.

[0032] Through this hydrogenation method, 60 tons / hour of qualified raw materials are added for the normal and iso-isomerization device, 20 t / h of pentane foaming agent is increased, 7 t / h of industrial iso-hexane is increased, and the economic benefits of the company are greatly improved.

[0033] The above only discloses the preferred embodiments of the present application, and of course cannot limit the scope of the rights of the present application, so the equivalent changes made according to the claims of the present application still fall within the scope covered by the present application.

Claims

1. A system for hydrogenative saturation of olefins in pentane oil components, characterized by: It includes hydrogen gas inlet pipeline (100) and pentane oil feed pipeline (101); the pentane oil feed pipeline (101) is connected to the hydrogenation reactor (5), and the pentane oil feed pipeline (101) is sequentially connected to the carbon four raw material buffer tank (1), hydrogenation feed pump (2), start-up heater (3) and raw material oil heat exchanger (4); the hydrogen gas inlet pipeline (100) is connected to the pentane oil feed pipeline (101), and the hydrogen gas inlet pipeline (100) is arranged between the start-up heater (3) and the raw material oil heat exchanger (4); the outlet of the hydrogenation reactor (5) is connected to the de-isobutane column (6) through the hydrogenation product discharge pipeline (102), and the start-up heater (3) is connected to the hydrogenation product discharge pipeline (102); the overhead outlet of the de-isobutane column (6) is connected to the overhead inlet of the de-isobutane column (6) through the overhead reflux pipeline (103), and the overhead air cooler (7), the overhead reflux tank (8) and the overhead reflux pump (9) are sequentially connected to the overhead reflux pipeline (103); the bottom outlet of the de-isobutane column (6) is connected to the normal isomerization device through the alkylate oil pipeline (104), and the alkylate oil separation tower air cooler (10), the alkylate oil separation tank reflux tank (11), the refrigerant circulating pump (12) and the light alkylate oil cooler (13) are sequentially connected to the alkylate oil pipeline (104).

2. The olefin hydro-saturation system in a pentane oil component of claim 1, wherein: The bottom outlet of the de-isobutane column (6) is connected to the bottom inlet of the de-isobutane column (6) through the bottom reflux pipeline (105), and the de-isobutane column bottom reboiler (14) is connected to the bottom reflux pipeline (105).

3. The olefin hydro-saturation system in a pentane oil component of claim 2, wherein: It also includes a condensate pipeline (106), which is sequentially connected to the de-isobutane column bottom reboiler (14) and the de-isobutane reboiler condensate tank (15).

4. The olefin hydro-saturation system in pentane oil components of claim 1, wherein: The tank top of the overhead reflux tank (8) is connected to the fuel gas pipeline network through the non-condensable gas pipeline (107), and a valve is arranged on the non-condensable gas pipeline (107).

5. The olefin hydro-saturation system in pentane oil components of claim 1, wherein: A first bypass line (108) is arranged on the pentane oil feed pipeline (101), the first bypass line (108) is connected between the front road and the rear road of the hydrogenation feed pump (2), and a second hydrogenation feed pump (17) is arranged on the first bypass line (108).

6. The olefin hydro-saturation system in pentane oil component of claim 1, wherein: A second bypass line (109) is arranged on the alkylate oil pipeline (104), the second bypass line (109) is connected between the front road and the rear road of the refrigerant circulating pump (12), and an alkylate oil separation tank reflux pump (16) is arranged on the second bypass line (109).

7. The olefin hydro-saturation system in pentane oil component of claim 1, wherein: A valve is arranged on the front road of the overhead air cooler (7), and a valve is arranged on the rear road of the overhead reflux pump (9); a valve is arranged on the front road of the alkylate oil separation tower air cooler (10), and a valve is arranged on the rear road of the light alkylate oil cooler (13).

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