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Stripped gas method for recovering C2 and higher carbon content hydrocarbon constituent

A dry gas and hydrocarbon technology, which is applied in the recovery of liquid hydrocarbon mixtures and the petroleum industry, can solve problems such as limited application range, investment, high operating cost, and difficult operation, and achieve practical operability and solve technical problems. Effect

Active Publication Date: 2006-07-12
SOUTHWEST RES & DESIGN INST OF CHEM IND
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

The former two are not widely popularized and applied due to the difficulty in operation, high investment and operating costs, and inconspicuous economic benefits; the adsorption separation method, especially the pressure swing adsorption (PSA) method, has become the domestic chemical industry due to its simple operation and low equipment cost. Cost-effective separation method widely used in factories
The C recovered in the existing dry gas pressure swing adsorption process 2 and C 2 Due to the high content of impurities such as sulfide and oxygen in the above hydrocarbon components, in subsequent applications, these impurities will easily reduce the activity of the catalyst, or even poison and lose its activity, affecting normal production, so it cannot be purified by the ethylene cryogenic rectification unit in the downstream factory Recovery of ethylene, propylene and ethylene cracking furnace feedstock ethane, propane, etc., thus limiting the recovery of ethylene, ethane and C from dry gas 2 The scope of application of the above hydrocarbon components

Method used

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  • Stripped gas method for recovering C2 and higher carbon content hydrocarbon constituent
  • Stripped gas method for recovering C2 and higher carbon content hydrocarbon constituent
  • Stripped gas method for recovering C2 and higher carbon content hydrocarbon constituent

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0026] This embodiment reclaims C from refinery catalytic cracking dry gas 2 and C 2 The method of the above hydrocarbon components, catalytic cracking dry gas treatment capacity 5000Nm 3 / h, pressure 0.55MPa, temperature 40°C, its gas composition is shown in Table 1:

[0027] composition

H 2

O 2

N 2

CH 4

CO

CO 2

C 2 h 4

C 2 h 6

C 3 h 6

C 3 h 8

C 4

C 5 +

h 2 S

Content %

25.8

0.3

9.1

30

0.9

1.5

13.5

12

4.2

0.8

0.8

1.1

50ppm

[0028] C in the table 4 Indicates hydrocarbon gases containing 4 carbon atoms, such as n-butane, isobutane, isobutene, n-butene, anti-butene; C 5 + Indicates hydrocarbon gases containing 5 and more carbon atoms.

[0029] In this embodiment, firstly, the pressure swing adsorption method is used to concentrate and separate the C in the catalytic cracking dry gas. 2 ...

Embodiment 2

[0045] Coking dry gas flow rate is 12000Nm 3 / h, pressure 0.7Mpa, temperature 30°C, its component content is shown in Table 4, and enters the pressure swing adsorption gas separation unit, MEA desulfurization and decarbonation unit, water washing and dehydration unit, water separation unit, fine dehydration unit, dehydration unit, Coking dry gas separation, purification and recovery C composed of arsenic unit, fine desulfurization unit and hydrodeoxygenation reactor unit 2 and C 2 The above hydrocarbon component device.

[0046] composition

H 2

O 2

N 2

CH 4

C 2 h 4

C 2 h 6

C 3 h 8

C 3 h 6

i-C 4

n-C 4

n-C 4 ＝

h 2 S

As

Content %

4.90

0.64

3.24

52.97

3.32

19.21

9.21

5.03

0.54

0.47

0.46

0.01

0.5ppm

[0047] Table i-C 4 , n-C 4 , n-C 4 ＝ Respectively represent isobutane, n-butane and n-buten...

Embodiment 3

[0064] Refinery catalytic cracking dry gas flow rate 25000Nm 3 / h, pressure 0.60MPa, temperature 30°C, its gas composition is shown in Table 7:

[0065] composition

H 2

O 2

N 2

CH 4

CO

CO 2

C 2 h 4

C 2 h 6

C 3 h 6

C 3 h 8

C 4

C 5 +

h 2 S

As

h 2 o

Content %

25.3

0.3

9.1

30

0.9

1.5

13.5

12

4.2

0.8

0.8

1.1

30ppm

2ppm

0.5

[0066] The catalytic cracking dry gas separation and purification device in this embodiment is as follows image 3 As shown, it consists of pressure swing adsorption unit, MDEA desulfurization and decarbonation unit, water washing and dehydration unit, water separation unit, fine dehydration unit, arsenic removal unit, fine desulfurization unit, hydrodeoxygenation reactor unit, alkali elution carbon dioxide unit 1. Water washing dealkalization unit, wate...

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PUM

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Abstract

The invention discloses a method for dry gas reclaiming C2 and C2 above hydrocarbon component. The dry gas at least uses the pressure swing adsorbing step which is formed by absorbing, inverse putting, air drafting and swashing to separate the C2 and C2 above hydrocarbon component; the gas after swashing and absorbing at least dose wet desulfurization, extract desulfurization and deoxidation steps to purify it to obtain the mixing gas of C2 and C2 above hydrocarbon component. The (V / V) sulfur content of the reclaiming C2 and C2 above hydrocarbon component is less than 0.1ppm and the oxygen content is less than 1ppm.

Description

technical field [0001] The invention relates to a method for separating, purifying and recovering useful gas components from mixed gas, in particular, to a method for separating and recovering C-rich components from dry gas. 2 and C 2 The method of the above hydrocarbon components. Background technique [0002] The catalytic cracking dry gas from the heavy oil catalytic cracking unit and the coking dry gas from the coking unit are rich in ethylene, ethane and C 2 The basic chemical raw material resources such as the above hydrocarbon components were used as fuel and burned in vain in the past because there was no industrial recovery technology. C in dry gas 2 and C 2 Concentration and recovery technologies for the above hydrocarbon components mainly include cryogenic separation, intercooled oil absorption separation and adsorption separation. The former two are not widely popularized and applied due to the difficulty in operation, high investment and operating costs, an...

Claims

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Application Information

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IPC IPC(8): C10G5/02
Inventor 张剑锋刘丽石江刘照利
Owner SOUTHWEST RES & DESIGN INST OF CHEM IND
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