Rich-phase regeneration device suitable for phase change absorbent
By using a combination of hollow fiber membrane module and flash tank in a phase-rich regeneration device of phase change absorber, the problem of mass transfer is solved, low-energy regeneration and efficient desorption are achieved, and industrial application prospects are available.
Patent Information
- Application Number
- CN202411299583.2
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2024-09-18
- Publication Date
- 2025-01-03
AI Technical Summary
The phase-rich phase of the phase change absorber is limited in traditional tower equipment, resulting in problems such as reduced desorption rate and equipment blockage, which increases equipment cost and energy consumption.
Using a device combining a hollow fiber membrane module and a flash tank, a phase-rich low-energy regeneration is achieved through heating and steam heat exchange, reducing the viscosity of the absorbent, and improving the mass transfer efficiency through the filler layer.
It effectively solves the problem of phase-rich phase-transfer of phase-change absorbers in traditional tower equipment, realizes low-energy regeneration of phase-change absorbers, improves the adsorption rate and equipment reliability, and reduces equipment costs.
Smart Images
Figure CN119236610A_ABST
Abstract
Description
Technical Field
[0001] The present invention relates to the technical field of carbon capture technology, in particular to a rich phase regeneration device suitable for a phase change absorbent. Background Art
[0002] Post-combustion capture technology is relatively mature. Chemical absorption has the advantages of high decarbonization efficiency and good selectivity. It is currently the most widely used post-combustion CO2 removal technology. The core of the chemical absorption method is the formulation development of organic amine solvents. The phase change absorbent forms two phases, rich and poor, after absorption. Compared with traditional composite amine absorbents, it has the advantages of low regeneration energy consumption and low corrosiveness. It is currently a hot research topic.
[0003] In industry, traditional tower equipment is generally used to regenerate and separate the absorbent. The process technology is mature and the operation is stable. It is regenerated by steam heating to achieve CO2 separation in the rich phase. The steam temperature is generally not higher than 130°C.
[0004] Phase change absorbent forms two phases, rich and poor, after absorbing CO2, which reduces the regeneration energy consumption. However, the rich phase entering the regeneration tower generally has a higher viscosity, which limits the mass transfer of the rich phase in traditional tower desorption equipment and affects the desorption rate. At the same time, excessive viscosity of the absorbent can easily cause problems such as blockage between pipelines, and can also cause damage to parts such as pumps, affecting their service life and increasing equipment costs. Summary of the invention
[0005] The purpose of the present invention is to solve the problems in the prior art and to propose a device suitable for regenerating the rich phase of a phase change absorbent, which can solve the problem of limited mass transfer of the rich phase of the phase change absorbent in traditional tower equipment, and realize low-energy regeneration of the phase change absorbent, and has industrial application prospects.
[0006] To achieve the above-mentioned purpose, the present invention proposes a phase-rich regeneration device suitable for phase-change absorbent, comprising a tank body, a hollow fiber membrane assembly, a flash tank I, a flash tank II and a plurality of packing layers I, wherein a hollow fiber membrane assembly is arranged in the upper end of the tank body, and the hollow fiber membrane assembly is provided with a rich liquid inlet, a pre-regeneration liquid outlet and a CO2 gas outlet, the absorbent rich liquid input by the rich liquid inlet is first heated to a certain temperature, the pre-regeneration liquid outlet is connected to the feed port of the flash tank I, the discharge port of the flash tank I is connected to the tank body, the steam output by the flash tank I is used to heat the semi-regenerated absorbent in the tank body, an absorbent lean liquid collection chamber is arranged at the lower end of the tank body, the steam outlet and the feed port of the flash tank II are connected to the absorbent lean liquid collection chamber, the absorbent lean liquid output by the discharge port of the flash tank II is sent to an absorption tower, and packing layers I are arranged at intervals in the middle of the tank body.
[0007] Preferably, the steam output from the steam outlet of the flash tank I exchanges heat with the gas in the tank body through the heat exchanger I, and the gas after heat exchange enters the tank body to heat the semi-regenerated absorbent passing through the corresponding packing layer I.
[0008] Preferably, a steam inlet is provided on the absorbent lean liquid collection chamber.
[0009] Preferably, a packing layer II is provided between two adjacent packing layers I in the tank body, and the packing layer II is a desorption catalyst packing.
[0010] Preferably, a mixed gas outlet is provided at the upper end of the tank body, and the mixed gas outlet is connected to the gas-liquid separator through the heat exchanger II.
[0011] Preferably, the joints of the hollow fiber membrane components are sealed with silicone glue.
[0012] Preferably, the heating temperature of the absorbent-rich liquid before entering the hollow fiber membrane module is 70-80°C.
[0013] Beneficial effects of the present invention: the present invention provides a hollow fiber membrane assembly with a rich liquid inlet, a pre-regeneration liquid outlet and a CO2 gas outlet, the absorbent rich liquid input into the rich liquid inlet is first heated to a certain temperature, the pre-regeneration liquid outlet is connected with the feed port of a flash tank I, the discharge port of the flash tank I is connected with the tank body, an absorbent lean liquid collecting chamber is provided at the lower end of the tank body, the steam outlet and the feed port of the flash tank II are connected with the absorbent lean liquid collecting chamber, the steam output from the flash tank I is used to heat the semi-regenerated absorbent in the tank body, the absorbent lean liquid output from the discharge port of the flash tank II is fed into an absorption tower, and a filler layer I arranged at intervals is provided in the middle of the tank body. Compared with the prior art, the present invention can solve the problems of limited mass transfer of the rich phase of the phase change absorbent in traditional tower equipment, and realize low-energy regeneration of the phase change absorbent, which has industrial application prospects.
[0014] The features and advantages of the present invention will be described in detail through embodiments in conjunction with the accompanying drawings. BRIEF DESCRIPTION OF THE DRAWINGS
[0015] Figure 1 It is a structural schematic diagram of a phase-change absorbent rich-phase regeneration device suitable for the present invention.
[0016] In the figure: 1-tank body, 2-hollow fiber membrane assembly, 3-flash tank I, 4-flash tank II, 5-packing layer I, 6-heat exchanger I, 7-absorbent lean liquid collection chamber, 8-steam inlet, 9-packing layer II, 10-mixed gas outlet, 11-heat exchanger II, 12-gas-liquid separator, 21-rich liquid inlet, 22-pre-regeneration liquid outlet, 23-CO2 gas outlet. DETAILED DESCRIPTION
[0017] See also Figure 1 The present invention discloses a phase-change absorbent rich phase regeneration device, comprising a tank body 1, a hollow fiber membrane assembly 2, a flash tank I3, a flash tank II4 and a plurality of packing layers I5. The upper end of the tank body 1 is provided with a hollow fiber membrane assembly 2, and the hollow fiber membrane assembly 2 is provided with a rich liquid inlet 21, a pre-regeneration liquid outlet 22 and a CO2 gas outlet 23. The absorbent rich liquid input by the rich liquid inlet 21 is first heated to a certain temperature, the pre-regeneration liquid outlet 22 is connected to the feed port of the flash tank I3, the discharge port of the flash tank I3 is connected to the tank body 1, the steam output by the flash tank I3 is used to heat the semi-regenerated absorbent in the tank body 1, the lower end of the tank body 1 is provided with an absorbent lean liquid collection chamber 7, the steam outlet and the feed port of the flash tank II4 are connected to the absorbent lean liquid collection chamber 7, the absorbent lean liquid output by the discharge port of the flash tank II4 is sent to an absorption tower, and the middle of the tank body 1 is provided with a packing layer I5 arranged at intervals.
[0018] The steam output from the steam outlet of the flash tank I3 exchanges heat with the gas in the tank body 1 through the heat exchanger I6, and the gas after heat exchange enters the tank body 1 to heat the semi-regenerated absorbent passing through the corresponding packing layer I5.
[0019] The absorbent lean liquid collecting chamber 7 is provided with a steam inlet 8 .
[0020] A packing layer II9 is provided between two adjacent packing layers I5 in the tank body 1, and the packing layer II9 is a desorption catalyst packing.
[0021] The upper end of the tank body 1 is provided with a mixed gas outlet 10 , and the mixed gas outlet 10 is connected to the gas-liquid separator 12 through a heat exchanger II11 .
[0022] The joints of the hollow fiber membrane assembly 2 are sealed with silicone glue.
[0023] The heating temperature of the absorbent-rich liquid before entering the hollow fiber membrane module 2 is 70-80°C.
[0024] Working process of the present invention: The present invention is applicable to a phase change absorbent rich phase regeneration device. During operation, the absorbent rich liquid is pumped from the phase separation tank into the hollow fiber membrane assembly 2 by a pump, and the outside is the gas phase after desorption. To ensure air tightness, the membrane assembly is sealed at the joint with silicone adhesive. The absorbent rich liquid is preheated before entering the membrane assembly, and the heating temperature does not exceed 80°C. The absorbent rich liquid separated by the membrane assembly has a low viscosity, and the mass transfer effect in the desorption tower is improved. After being pretreated by the membrane assembly, it enters the flash tank I3 for flash evaporation. The pretreated absorbent rich liquid entering the flash tower will be instantly vaporized in large quantities under the condition of reduced pressure, and the secondary steam generated will pass through the heat exchanger I6 It exchanges heat with the gas in the tank body 1. The gas after heat exchange enters the tank body 1 to heat the absorbent rich liquid passing through the corresponding packing layer I5. After heat exchange, it is returned to the bottom of the desorption tower for regeneration using a direct steam method. In addition to the packing layer I5 for increasing mass transfer, the desorption tower is also provided with two sections of packing layers II9 for improving the regeneration efficiency of the rich liquid during the residence time of the desorption tower. The lean liquid formed after regeneration is gathered in the absorbent lean liquid collection chamber 7 with a high temperature. The heat is recovered through the flash tank II4, and the generated steam can be reused for the regeneration of the absorbent rich liquid in the desorption tower, thereby reducing the amount of steam used for regeneration, thereby achieving low-energy regeneration of the phase change absorbent rich liquid.
[0025] Since the membrane flash evaporation process can effectively reduce the viscosity of the rich phase and lower the regeneration temperature, it is suitable for the regeneration of the rich phase of the phase change absorbent. However, the lean liquid obtained by a single separation may have a problem of too high CO2 load, resulting in a low absorbent circulation load, affecting the capture efficiency. The present invention adopts a membrane flash evaporation process to replace the reboiler part of the traditional tower desorption equipment, and on the basis of the membrane flash evaporation process, the steam output by the flash tank I3 is used to heat the semi-regenerated absorbent in the tank body 1, and is connected to the absorbent lean liquid collection chamber 7 through the steam outlet and the feed port of the flash tank II4. The absorbent lean liquid output from the discharge port of the flash tank II4 is sent to the absorption tower, which solves the problem of limited mass transfer of the rich phase of the phase change absorbent in the traditional tower equipment, and realizes low-energy regeneration of the phase change absorbent, which has industrial application prospects.
[0026] The above embodiments are intended to illustrate the present invention, not to limit the present invention. Any solution that is a simple transformation of the present invention belongs to the protection scope of the present invention.
Claims
1. A rich phase regeneration device suitable for phase change absorbent, characterized in that: The invention comprises a tank body (1), a hollow fiber membrane assembly (2), a flash tank I (3), a flash tank II (4) and a plurality of packing layers I (5). The upper end of the tank body (1) is provided with a hollow fiber membrane assembly (2). The hollow fiber membrane assembly (2) is provided with a rich liquid inlet (21), a pre-regeneration liquid outlet (22) and a CO2 gas outlet (23). The absorbent rich liquid inputted into the rich liquid inlet (21) is first heated to a certain temperature. The pre-regeneration liquid outlet (22) is connected to the inlet of the flash tank I (3). The feed inlet of the flash tank I (3) is connected to the tank body (1), the discharge port of the flash tank I (3) is connected to the tank body (1), the steam output from the flash tank I (3) is used to heat the semi-regenerated absorbent in the tank body (1), the lower end of the tank body (1) is provided with an absorbent lean liquid collection chamber (7), the steam outlet and the feed inlet of the flash tank II (4) are connected to the absorbent lean liquid collection chamber (7), the absorbent lean liquid output from the discharge port of the flash tank II (4) is sent to the absorption tower, and a filler layer I (5) arranged at intervals is provided in the middle of the tank body (1).
2. A phase-rich regeneration device for phase-change absorbent as claimed in claim 1, characterized in that: The steam output from the steam outlet of the flash tank I (3) exchanges heat with the gas in the tank body (1) through the heat exchanger I (6), and the gas after heat exchange enters the tank body (1) to heat the semi-regenerated absorbent passing through the corresponding packing layer I (5).
3. A phase-rich regeneration device for phase-change absorbent as claimed in claim 1, characterized in that: The absorbent lean liquid collection chamber (7) is provided with a steam inlet (8).
4. A phase-rich regeneration device for phase-change absorbent as claimed in claim 1, characterized in that: A packing layer II (9) is provided between two adjacent packing layers I (5) in the tank body (1), and the packing layer II (9) is a desorption catalyst packing.
5. A rich phase regeneration device for phase change absorbent as claimed in claim 1, characterized in that: A mixed gas outlet (10) is provided at the upper end of the tank body (1), and the mixed gas outlet (10) is connected to the gas-liquid separator (12) via a heat exchanger II (11).
6. A phase-rich regeneration device for phase-change absorbent as claimed in claim 1, characterized in that: The joints of the hollow fiber membrane components (2) are sealed with silicone glue.
7. A rich phase regeneration device for phase change absorbent according to any one of claims 1 to 6, characterized in that: The heating temperature of the absorbent-rich liquid before entering the hollow fiber membrane module (2) is 70-80°C.