Alkylation reaction apparatus, reaction system, and liquid acid catalyzed alkylation reaction process

Patent metadata

Field	Value
Publication number	US-11890589-B2
Application number	US-202017433190-A
Country	US
Kind code	B2
Filing date	Feb 21, 2020
Priority date	Feb 21, 2019
Publication date	Feb 6, 2024
Grant date	Feb 6, 2024

Abstract

An alkylation reaction apparatus has n reactors. In the n reactors, there are m reactors including the first reactor that have three reaction zones as defined below. According to the flow direction order of alkylation reaction streams, the three reaction zones are an x reaction zone, a y reaction zone and a z reaction zone respectively; based on the mixing intensity, the mixing intensity of the y reaction zone>the mixing intensity of the x reaction zone>the mixing intensity of the z reaction zone, wherein n≥1 and n≥m. An alkylation reaction system includes the aforementioned alkylation reaction apparatus, and a liquid acid catalyzed alkylation reaction process by using the aforementioned alkylation reaction apparatus or the aforementioned alkylation reaction system.

First claim

The invention claimed is:

1. An alkylation reaction apparatus, comprising n reactors, wherein m reactors among the n reactors, including a first reactor that are those having each comprises three reaction zones,
said three reaction zones being an x reaction zone, a y reaction zone, and a z reaction zone arranged in a direction along a flow direction of an alkylation reaction streams, and
wherein the y reaction zone has a mixing intensity greater than a mixing intensity of the x reaction zone, and the mixing intensity of the x reaction zone is greater than a mixing intensity of z reaction zone, wherein n≥1 and n≥m.

2. The apparatus of claim 1 , wherein n is 2, 3, 4, 5, 6, 7, or 8.

3. The apparatus according to claim 1 , wherein the X reaction zone, the y reaction zone, and the z reaction zone have inner diameters of Rx, Ry, and Rz, respectively.

4. The apparatus according to claim 1 , wherein at least one of the x reaction zone, the y reaction zone, and the z reaction zone is provided with one or more flow disturbance component.

5. The apparatus according to claim 1 , wherein said n reactors are connected in series and/or in parallel.

6. An alkylation reaction system comprising an alkylation reaction unit, a compression refrigeration unit, a reaction effluent refining unit, and a product fractionation unit, wherein the alkylation reaction unit comprises the alkylation reaction apparatus according to claim 1 .

7. The reaction system according to claim 6 , wherein,
the alkylation reaction apparatus is provided with a mixer for receiving a diluted alkylation reaction raw material, wherein the diluted alkylation reaction raw material is obtained by mixing an alkylation reaction raw material with an isobutane refrigerant obtained from the compression refrigeration unit, a recycled isobutane obtained from the product fractionation unit and a recycled hydrocarbon obtained from the reaction effluent refining unit;
a reaction effluent is subjected to a preliminary separation of acid and hydrocarbon in the reaction effluent refining unit, and a majority of a resulting hydrocarbon phase is used as the recycled hydrocarbon; and
a product fractionation unit comprises at least one deisobutanizer, in which isobutane in the hydrocarbon phase of the reaction effluent is removed, and a recycled isobutane, normal butane and an alkylation product are respectively obtained from a top of the deisobutanizer, a middle upper part of the deisobutanizer, and a bottom of the deisobutanizer.

8. The reaction system according to claim 6 , wherein the reaction effluent refining unit comprises a self-vaporization separator and a preliminary acid-hydrocarbon separator,
wherein a coalescing internal member is arranged at an upper part of the self-vaporization separator for vaporizing butane and separating a reaction product from an acid phase, and an acid-hydrocarbon phase homogenizer is arranged at a lower part of the self-vaporization separator, and
where the preliminary acid-hydrocarbon separator is used for performing a primary separation of acid and hydrocarbon, a majority of the separated hydrocarbon phase is recycled, and a minority of the hydrocarbon phase is optionally subjected to a further coalescence-deacidification separation.

9. The reaction system according to claim 6 , further comprises an alkylation reaction raw material pretreatment unit in which butadiene, light hydrocarbons, oxygen-containing compounds and water are removed from the alkylation reaction raw material.

10. The apparatus of claim 2 , wherein n is 3 or 4, m is 2 or 3.

11. The apparatus according to claim 4 , wherein the ratio of the inner diameter of the z reaction zone to the inner diameter of the x reaction zone to the inner diameter of the y reaction zone is Rz reaction zone: Rx reaction zone: Ry reaction zone=(2-5):(1.1-1.8):1.

12. The apparatus according to claim 4 , wherein the internal flow disturbance component is a static flow disturbance component or a dynamic flow disturbance component.

13. The apparatus according to claim 12 , wherein the static flow disturbance component is selected from CompaX Mixer, SMI Mixer, KVM Mixer, SMV Mixer, SMX plus Mixer, SMXL Mixer, SMR Mixer, SMX Mixer, SMR Reactor, Contour Mixer, SMF Mixer, Polygard Mixer, KM Mixer, KMX-V Mixer, HEV Mixer, UltraTab Mixer, WVM Mixer, SV, SH, SK, SX, SL, and Toray Hi-Type.

14. The apparatus according to claim 5 , wherein n=3, m=3 or 2, the reactors are connected in series in an N-type manner; or n=4, m=4, or 3, or 2, the reactors are connected in series in an M-type manner.

15. A liquid acid catalyzed alkylation reaction process, wherein the alkylation reaction of isobutane with a C3-C5 alkene fraction is carried out in the presence of a liquid acid in n reactors, and a inlet temperature of a first reactor amongst said n reactors is −10° C. to 20° C.,
m reactors among said n reactors, including the first reactor, are each provided with an x reaction zone, a y reaction zone and a z reaction zone;
a diluted alkylation reaction raw material is distributed to said m reactors,
in each of said m reactors, an alkylation reaction stream firstly flows into the x reaction zone and then successively flows through the y reaction zone and the z reaction zone, and a mixing intensity of the y reaction zone is greater than a mixing intensity of the x reaction zone, which is greater than a mixing intensity of the z reaction zone, wherein n≥1 and n≥m;
the reaction stream has a residence time in the x reaction zone of 0.01-10 seconds, a residence time in they reaction zone of 0.01-10 seconds, and a residence time in the z reaction zone of 0.1-15 minutes.

16. The reaction process according to claim 15 , wherein the diluted alkylation reaction raw material comprises a recycled isobutane, an isobutane refrigerant, an optionally pretreated alkylation reaction raw material, and a recycled hydrocarbon, and a molar ratio of alkane to alkene in the diluted alkylation reaction raw material is 10-300:1.

17. The reaction process according to claim 15 , wherein:
a reaction effluent obtained from an outlet of the nth reactor is depressurized to 0.005-0.18 MPa by a coalescing internal member in a self-vaporization separator, so that a part of C4 alkanes in the reaction effluent is vaporized,
gas phase components from the reaction effluent are separated, compressed and refrigerated to obtain an isobutane refrigerant, the remainder of the reaction effluent is separated into an acid phase and a hydrocarbon phase in a lower part of the self-vaporization separator, and the acid phase is recycled back to the x reaction zone of the first reactor, a majority of the hydrocarbon phase is sent to a raw material mixer, and a minority of the hydrocarbon phase is sent to an optional precision coalescer to further remove acid and acid esters in the hydrocarbon phase;
wherein isobutane in the hydrocarbon phase of the reaction effluent is removed in a deisobutanizer, and the recycled isobutane, normal butane and an alkylation product are obtained from a top of the deisobutanizer, a middle upper part of the deisobutanizer, and a bottom of the deisobutanizer, respectively.

18. The process according to claim 15 , wherein in the x reaction zone and in the y reaction zone, the pressure drop is 0.05-0.5 MPa, and in the z reaction zone, the pressure drop is 0.001-0.1 MPa.

19. The process according to claim 15 , wherein the liquid acid comprising a concentrated sulfuric acid
and optionally an auxiliary agent, wherein, when the auxiliary agent is present, has a weight

Assignees

• China Petroleum & Chem Corp
• Sinopec Res Inst Petroleum

Inventors

• Dong Minghui
• Zong Baoning
• Mu Xuhong
• Luo Yibin
• Chen Hua
• Zheng Jinyu
• Wen Langyou

Classifications

• B01J19/0053 Primary

  Details of the reactor · CPC title

• B01D3/009

  in combination with chemical reactions · CPC title

• B01J19/1806

  resulting in a turbulent flow of the reactants, such as in centrifugal-type reactors, or having a high Reynolds-number · CPC title

• C07C2/62

  with acids · CPC title

• B01J2219/0004

  Processes in series · CPC title