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C2 fraction selective hydrogenation method

A selective hydrogenation and fractionation technology, which is applied in the fields of hydrocarbons, chemical instruments and methods, and hydrogenation hydrocarbon production, can solve the problems of migration and aggregation of metal particles and the inability to form strong interactions, and achieve significant economic benefits and facilitate smooth operation , the effect of widening the operating range

Active Publication Date: 2013-07-31
PETROCHINA CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

In addition, after impregnation, no strong interaction can be formed between the metal salt species and the carrier, and high-temperature calcination easily leads to the migration and aggregation of metal particles to form large grains.

Method used

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  • C2 fraction selective hydrogenation method
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  • C2 fraction selective hydrogenation method

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0044] The reaction material comes from the front depropanizer, and the composition of the raw material is shown in Table 1:

[0045] Table 1 hydrogenation raw material composition

[0046] Hydrogenation feedstock

H 2

C 2 h 2

C 2 h 4

C 2 h 6

CH 4

C 3 h 6

C 3 h 8

PDMA

CO

C 4 +

Content (v%)

21

0.64

34

4.36

23

14

2

0.50

0.2

0.3

[0047] Reaction process conditions: single reactor material volume space velocity: 25000h -1 ; Operating pressure: 3.9MPa; Catalyst loading capacity of each reactor: 500ml.

[0048] Adiabatic bed reactor, three-stage series process, and other process conditions are shown in Table 2.

[0049] The catalyst used is prepared by the method obtained in the present invention.

[0050] Weigh 500g of the carrier, the carrier is spherical Al 2 o 3 , with a specific surface area of ​​30m 2 / g, the pore volume is...

Embodiment 2

[0064] Reaction process conditions: pre-depropanization pre-hydrogenation process.

[0065] Material air speed: 10000h -1 , Operating pressure: 3.5MPa, single-stage adiabatic bed reactor, catalyst loading: 800ml.

[0066] The hydrogenation reaction material comes from the top of the front depropanizer, and its composition is shown in Table 3.

[0067] Table 3 hydrogenation raw material composition

[0068] Hydrogenation feedstock

H 2

C 2 h 2

C 2 h 4

C 2 h 6

CH 4

CO

C 3 h 6

C 3 h 8

PDMA

Content (V%)

20

1.0

40.68

6..8

17

0.02

12

2

0.50

[0069] Catalyst preparation:

[0070] Weighing length is 4.5mm, specific surface area is 2m 2 / g, the pore volume is 0.20ml / g, the bulk density is 1.2g / cm 3 Cylindrical Al2 o 3 Carrier 500g.

[0071] Weigh 0.60g Pd(NO 3 ) 2 2H 2 O, 5.27g Mg(NO 3 ) 2 ·6H 2 O, 4.8g g urea, is dissolved in deionized w...

Embodiment 3

[0085] Reaction process conditions: pre-depropanization and pre-hydrogenation process, two-stage adiabatic reactor; single-stage or each-stage material volume space velocity: 3000h -1 ;Operating pressure: 4.5MPa, each catalyst filling volume: 300ml.

[0086] The raw material for hydrogenation also comes from the front depropanizer, and its composition is shown in Table 5.

[0087] Table 5 hydrogenation raw material composition

[0088] Hydrogenation feedstock

H 2

C 2 h 2

C 2 h 4

C 2 h 6

CH 4

C 3 h 6

C 3 h 8

PDMA

CO

C 4 +

Content (v%)

15

0.4

32

4.28

30

15

2.3

0.7

0.02

0.3

[0089] Weigh spherical Al 2 o 3 Carrier 500g, its specific surface area is 10.3m 2 / g, the pore volume is 0.40ml / g, the bulk density is 1.1g / cm 3 .

[0090] Weigh 0.47g Pd(NO 3 ) 2 2H 2 O, 23g Mg(NO 3 ) 2 ·6H 2 O, 3.1g of urea is prepared into a mix...

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Abstract

The invention provides a C2 fraction selective hydrogenation method, which utilizes a front-end hydrogenation process method of front-end depropanization. The method is characterized in that a Pd-Ag catalyst is filled in a fixed bed reactor, takes Al2O3 as a carrier, and contains 0.01-0.1% percent of Pd and 0.01-0.2% of Ag calculated according to the mass of the catalyst; an oxyhydrogen titrationmethod is used to measure the total metal dispersion degree of Pd and Ag in the catalyst, and the total metal dispersion degree is 35-65%; the fixed bed reactor is a heat insulation bed reactor the reaction condition of which is as follows: the inlet temperature of the reactor is 45-100 DEG C, the reaction pressure is 3.5-4.5MPa, and the gaseous hourly space velocity is 3000-25000h<-1>. The catalyst of the method has large operation range and strong adaptability to different process conditions, thereby being more beneficial to stable operation of devices and improving the yield of ethylene-propylene.

Description

technical field [0001] The invention relates to a method for selective hydrogenation, in particular to a method for selective hydrogenation of carbon distillates to remove acetylene. Background technique [0002] The production of ethylene is the leader of the petrochemical industry. The selective hydrogenation of acetylene in steam cracking products plays an extremely important role in the ethylene processing industry. In addition to ensuring that the content of acetylene at the outlet of the hydrogenation reactor meets the standard, the selectivity of the catalyst is excellent. It can make ethylene produce as little ethane as possible, which is of great significance to improving the ethylene yield in the whole production process and improving the economic benefit of the device. [0003] In the current carbon distillate hydrogenation to remove alkynes, more and more carbon distillate pre-hydrogenation processes are used. The feature of this process method is that the hydrog...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C11/04C07C11/06C07C7/163C07C7/167C07C5/09C07C5/05B01J23/50B01J37/00
CPCY02P20/52
Inventor 谭都平赵育榕龚光碧车春霞梁琨景喜林何颖马建华
Owner PETROCHINA CO LTD
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