Method and apparatus for recovering ethylene from fluidized catalytic cracking (FCC) off-gas

• US 9,090,522 B2
• Filed: 08/26/2011
• Issued: 07/28/2015
• Est. Priority Date: 08/26/2010
• Status: Active Grant

• Current Assignee: Korea Institute of Energy Research, SK Innovation Company Limited
• Original Assignee: Korea Institute of Energy Research, SK Innovation Company Limited
• Inventors: Park, Jong Ho, Kim, Jong Nam, Beum, Hee Tae, Lee, Seong Jun, Lee, Jang Jae, Kim, Dong Wook, Ko, Chang Hyun, Han, Sang Sup, Cho, Soon Haeng
• Primary Examiner(s): Nguyen, Tam M
• Application Number:
  US13/819,021
• Publication Number:
  US 20140148634A1
• Time in Patent Office: 1,432 Days
• Field of Search: None
• US Class Current: 1/1
• CPC Class Codes: B01D 2253/108 Zeolites
• CPC Class Codes: B01D 2256/24 Hydrocarbons
• CPC Class Codes: B01D 2257/7022 Aliphatic hydrocarbons
• CPC Class Codes: B01D 2259/40073 Ten
• CPC Class Codes: B01D 2259/4063 using seven beds
• CPC Class Codes: B01D 53/047 Pressure swing adsorption
• CPC Class Codes: C07C 11/04 Ethylene
• CPC Class Codes: C07C 7/12 by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
• CPC Class Codes: C07C 7/13 by molecular-sieve technique
• CPC Class Codes: C10G 2300/107 Atmospheric residues having a boiling point of at least about 538 °C
• CPC Class Codes: C10G 2300/4081 Recycling aspects
• CPC Class Codes: C10G 2400/20 C2-C4 olefins
• CPC Class Codes: C10G 70/046 by adsorption, i.e. with the use of solids
• CPC Class Codes: Y02C 20/20 of methane
• CPC Class Codes: Y02P 30/40 Ethylene production

Abstract

A method and apparatus for concentrating and recovering ethylene from the off-gas from an apparatus which produces gasoline, propylene and the like by fluidized catalytic cracking (FCC) of heavy oils such as atmospheric residue, generated in a crude oil refining process, is provided. The method and apparatus can reduce the amount of ethylene rinse in the subsequent ethylene displacement desorption process by increasing the ethylene purity of a raw material gas and reducing the concentration of weakly adsorbing components in the raw material gas and can reduce the loss of a desorbent during a distillation process for separating the desorbent from the weakly adsorbing components. Thus, ethylene can be recovered from the off-gas from fluidized catalytic cracking of heavy oils at high concentration and low cost.

Claims

1. A method for recovering ethylene from off-gas of a process for fluidized catalytic cracking (FCC) of a heavy oil fraction, the method comprising the processes of:

concentrating C2+ components of the FCC off-gas using a pressure swing adsorption process to obtain a C2+ rich mixed gas; and

introducing the C2+ rich mixed gas into a displacement desorption process to recover high-concentration ethylene from the mixed gas.

2. The method of claim 1, wherein the process of concentrating the C2+ components of the FCC off-gas using the pressure swing adsorption process comprises the steps of:

i) introducing the FCC off-gas into an adsorption column packed with an adsorbent selectively adsorbing the C2+ components, so that the C2+ components are adsorbed onto the adsorbent and the remaining impurities are discharged out of the adsorption column;

ii) discharging impurities from the adsorption column that was subjected to step i), by cocurrent depressurization;

iii) countercurrently depressurizing the adsorption column that was subjected to step ii), while obtaining a partially concentrated C2 component;

iv) recycling a portion of a gas discharged from the adsorption step into the adsorption column that was subjected to step iii), by low-pressure rinse, thereby desorbing C2+ components from the adsorption column;

v) recycling a gas discharged from the adsorption step into the adsorption column that was subjected to step iv), and pressurizing the adsorption column; and

vi) recycling a portion of a gas discharged from the adsorption step into the adsorption column that was subjected to step v), and pressurizing the adsorption column to the adsorption pressure.

3. The method of claim 1, wherein the process of concentrating the C2+ components of the FCC off-gas by the pressure swing adsorption process comprises the steps of:

i) introducing the FCC off-gas into an adsorption column packed with an adsorbent selectively adsorbing the C2+ components, so that the C2+ components are adsorbed onto the adsorbent and the remaining impurities are discharged out of the adsorption column;

ii) compressing a portion of a C2 rich stream obtained from countercurrent depressurization and low-pressure rinse and cocurrently introducing the compressed stream into the adsorption column that was subjected to step i), thereby rinsing impurities away from the adsorption column with a C2 rich stream pressurized by a compressor so that the inside of the adsorption column becomes a C2+ rich atmosphere;

iii) discharging impurities from the adsorption column that was subjected to step ii), by cocurrent depressurization;

iv) countercurrently depressurizing the adsorption column that was subjected to step iii), while obtaining a partially concentrated C2 component;

v) recycling a portion of a gas discharged from step i) into the adsorption column that was subjected to step iv), thereby desorbing C2+ components from the adsorption column by low-pressure rinse; and

vi) recycling a gas discharged from step i) into the adsorption column that was subjected to step iv), and pressurizing the adsorption column to the adsorption pressure.

4. The method of claim 2, wherein each of steps i) to vi) is periodically repeated in at least two adsorption columns.

5. The method of claim 2, wherein the adsorbent selectively adsorbing the C2+ components is selected from the group consisting of silica gel, zeolite and activated carbon.

6. The method of claim 1, wherein the process of introducing the C2+ rich mixed gas into the displacement desorption process to recover high-concentration ethylene comprises:

i) recovering gases resulting from adsorption and ethylene rinse into an adsorption column packed with an ethylene selective adsorbent;

ii) introducing the C2+ rich mixed gas into the ethylene selective adsorbent-packed adsorption column to adsorb ethylene from the mixed gas, and introducing unadsorbed components and a desorbent, fed into the adsorption column during desorption, through the outlet of the adsorption column into a distillation column that separates an ethylene-poor stream/desorbent mixture into components;

iii) introducing a high-concentration ethylene, obtained in a distillation column for separating an ethylene rich stream/desorbent mixture into components, into the adsorption column that was subjected to step ii), thereby removing ethane and other gases; and

iv) introducing a desorbent into the adsorption column that was subjected to step iii) so as to desorb ethylene from the adsorption column, and then sending the desorbed ethylene into the distillation column for separating the ethylene rich stream/desorbent mixture into components, thereby producing concentrated ethylene.

7. The method of claim 1, wherein the process of introducing the C2+ rich mixed gas into the displacement desorption process to recover high-concentration ethylene comprises:

i) introducing the C2+ rich mixed gas into the ethylene selective adsorbent-packed adsorption column to adsorb ethylene from the mixed gas, and introducing unadsorbed components and a desorbent, fed into the adsorption column during desorption, through the outlet of the adsorption column into a distillation column that separates an ethylene-poor stream/desorbent mixture into components;

ii) recovering gases resulting from ethylene rinse into an adsorption column packed with an ethylene selective adsorbent;

iii) introducing a high-concentration ethylene, obtained in a distillation column for separating an ethylene rich stream/desorbent mixture into components, into the adsorption column that was subjected to step ii), thereby removing ethane and other gases; and

iv) introducing a desorbent into the adsorption column that was subjected to step iii) so as to desorb ethylene from the adsorption column, and then sending the desorbed ethylene into the distillation column for separating the ethylene rich stream/desorbent mixture into components, thereby producing concentrated ethylene.

8. The method of claim 6, wherein each of steps i) to iv) is periodically repeated in at least two adsorption columns.

9. The method of claim 6, wherein, if the pressure in step ii) is higher than atmospheric pressure, the method further comprises, before step iii), a step of discharging components other than ethylene by cocurrent depressurization.

10. The method of claim 6, wherein the method further comprises the steps of:

v) communicating the adsorption column that was subjected to step i) with the adsorption column that was subjected to step iv) so as to send components other than ethylene from the adsorption column that was subjected to step i) to the adsorption column that was subjected to step (iv), thereby depressurizing the adsorption column that was subjected to step i) and pressurizing the adsorption column that was subjected to step v);

vi) discharging components other than ethylene from the adsorption columns that was subjected to step v), by cocurrent depressurization; and

vii) introducing the C2+ rich mixed gas into the adsorption columns that was subjected to step (vi), and pressurizing the adsorption columns to adsorption pressure.

11. The method of claim 6 or 7, wherein the ethylene selective adsorbent is a π

-complex adsorbent selectively forming a π

-complex with ethylene, a zeolite X adsorbent, a zeolite Y adsorbent, or a zeolite A adsorbent.

12. The method of claim 11, wherein the zeolite X adsorbent is a zeolite 13X adsorbent.

13. The method of claim 6, wherein the desorbent is a C3-C6 hydrocarbon.

14. The method of claim 6, wherein step iv) is carried out under conditions of a pressure of 1-10 atm and a temperature of 20-150°

C.

15. The method of claim 6, wherein the desorbent obtained in the distillation column for separating the ethylene-poor stream/desorbent mixture into components and in the distillation column for separating the ethylene rich stream/desorbent mixture into components is recycled to the adsorption column.

16. The method of claim 3, wherein each of steps i) to vi) is periodically repeated in at least two adsorption columns.

17. The method of claim 3, wherein the adsorbent selectively adsorbing the C2+ components is selected from the group consisting of silica gel, zeolite and activated carbon.

18. The method of claim 7, wherein each of steps i) to iv is periodically repeated in at least two adsorption columns.

19. The method of claim 7, wherein, if the pressure in step ii) is higher than atmospheric pressure, the method further comprises, before step iii), a step of discharging components other than ethylene by cocurrent depressurization.

20. The method of claim 7, wherein the method further comprises the steps of:

v) communicating the adsorption column that was subjected to step i) with the adsorption column that was subjected to step iv) so as to send components other than ethylene from the adsorption column that was subjected to step i) to the adsorption column that was subjected to step (iv), thereby depressurizing the adsorption column that was subjected to step i) and pressurizing the adsorption column that was subjected to step v);

vi) discharging components other than ethylene from the adsorption columns that was subjected to step v), by cocurrent depressurization; and

vii) introducing the C2+ rich mixed gas into the adsorption columns that was subjected to step (vi), and pressurizing the adsorption columns to adsorption pressure.

21. The method of claim 7, wherein the ethylene selective adsorbent is a π

-complex adsorbent selectively forming a π

-complex with ethylene, a zeolite X adsorbent, a zeolite Y adsorbent, or a zeolite A adsorbent.

22. The method of claim 21, wherein the zeolite X adsorbent is a zeolite 13X adsorbent.

23. The method of claim 7, wherein the desorbent is a C3-C6 hydrocarbon.

24. The method of claim 7, wherein step iv) is carried out under conditions of a pressure of 1-10 atm and a temperature of 20-150°

C.

25. The method of claim 7, wherein the desorbent obtained in the distillation column for separating the ethylene-poor stream/desorbent mixture into components and in the distillation column for separating the ethylene rich stream/desorbent mixture into components is recycled to the adsorption column.