CN115608112A - Based on flue gas CO 2 Purification regeneration energy-saving process - Google Patents
Based on flue gas CO 2 Purification regeneration energy-saving process Download PDFInfo
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- CN115608112A CN115608112A CN202211465307.XA CN202211465307A CN115608112A CN 115608112 A CN115608112 A CN 115608112A CN 202211465307 A CN202211465307 A CN 202211465307A CN 115608112 A CN115608112 A CN 115608112A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 50
- 239000003546 flue gas Substances 0.000 title claims abstract description 50
- 238000000034 method Methods 0.000 title claims abstract description 36
- 230000008929 regeneration Effects 0.000 title claims abstract description 31
- 238000011069 regeneration method Methods 0.000 title claims abstract description 31
- 238000000746 purification Methods 0.000 title claims abstract description 27
- 238000010521 absorption reaction Methods 0.000 claims abstract description 157
- 239000007788 liquid Substances 0.000 claims abstract description 65
- 239000007789 gas Substances 0.000 claims abstract description 16
- 239000012535 impurity Substances 0.000 claims abstract description 14
- 238000005507 spraying Methods 0.000 claims abstract description 13
- 238000000926 separation method Methods 0.000 claims abstract description 10
- 238000003795 desorption Methods 0.000 claims abstract description 5
- 239000002250 absorbent Substances 0.000 claims abstract description 4
- 230000002745 absorbent Effects 0.000 claims abstract description 4
- 238000006243 chemical reaction Methods 0.000 claims abstract description 4
- 238000010438 heat treatment Methods 0.000 claims abstract description 4
- 238000005728 strengthening Methods 0.000 claims abstract description 3
- 239000000428 dust Substances 0.000 claims description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 5
- 239000007921 spray Substances 0.000 claims description 5
- 229910002651 NO3 Inorganic materials 0.000 claims description 4
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 4
- 229910052717 sulfur Inorganic materials 0.000 claims description 4
- 239000011593 sulfur Substances 0.000 claims description 4
- 238000006276 transfer reaction Methods 0.000 claims description 2
- 238000012546 transfer Methods 0.000 abstract description 2
- 239000002351 wastewater Substances 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 43
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 14
- 230000001105 regulatory effect Effects 0.000 description 14
- 238000012544 monitoring process Methods 0.000 description 8
- 229910002092 carbon dioxide Inorganic materials 0.000 description 7
- 230000000694 effects Effects 0.000 description 7
- 238000004090 dissolution Methods 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 238000009423 ventilation Methods 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000011278 co-treatment Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 230000004083 survival effect Effects 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1431—Pretreatment by other processes
- B01D53/1437—Pretreatment by adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1431—Pretreatment by other processes
- B01D53/145—Pretreatment by separation of solid or liquid material
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Abstract
The invention discloses a flue gas-based CO 2 The regeneration energy-saving process for purification comprises the following steps: removing impurities: will contain CO 2 The flue gas is introduced into the purification cavity to remove impurities in the flue gas, and the CO after impurity removal is carried out 2 Introducing into an absorption tower; step two: CO2 2 The absorption of (2): spraying barren solution into two absorption cavities of the absorption tower to enable the barren solution to be in countercurrent contact with the flue gas, and finishing CO 2 Absorbing to obtain a pregnant solution; step three: CO2 2 Absorption of (2): heating the rich liquid, introducing the heated rich liquid into a supergravity reactor, and strengthening the relative speed and mutual contact between phases by using the flowing behavior of a multi-phase flow system under the supergravity condition, thereby realizing the mass and heat transfer process and the chemical reaction process, and enabling CO to react 2 Rapid desorption from the absorbent; step four: separation: the desorbed regeneration gas enters a separator for separation to obtain product gas to be discharged; desorbed barren solutionThe waste water is led into an absorption tower for secondary absorption or discharge, and the whole process is energy-saving and environment-friendly.
Description
Technical Field
The invention relates to the technical field of environmental protection, in particular to a flue gas-based CO 2 A regeneration energy-saving process for purification.
Background
In recent years, the atmospheric environment is continuously deteriorated by the burning of fossil fuels, and the "greenhouse effect" caused thereby is increasingly threatening human survival. CO2 2 Not only are major contributors to greenhouse gases, their hazards last longer. To alleviate the effect of "greenhouse effect", the first solution to CO should be 2 The emission reduction and the recycling are realized.
The carbon capture and sequestration technique is to reduce the emission of CO into the atmosphere without reducing the current fossil fuel usage 2 The most direct and efficient way of gas volume.
The method for separating carbon dioxide from flue gas by the CCS technology mainly comprises the following steps: membrane separation, physical adsorption, cryogenic distillation, absorption separation, and the like. CO capture by chemical absorption 2 The method is widely used due to the high absorption rate, high absorption efficiency, simple process and mature technology, and a plurality of demonstration evaluation projects are built at home and abroad. CO capture by chemical absorption 2 The main disadvantage of the technology is the high energy consumption of the regeneration system, in order to reduce CO 2 Regeneration energy consumption and CO reduction 2 The application provides a regeneration energy-saving process based on flue gas CO2 purification.
Disclosure of Invention
The invention aims to provide a flue gas-based CO 2 The regeneration energy-saving process for purification is characterized by that the absorption tower is formed into a whole body formed from main absorption cavity body and auxiliary absorption cavity body, under the condition of normal use, the main absorption cavity body is made of CO 2 The main absorption cavity absorbs CO through the auxiliary absorption cavity 2 Further CO is carried out when the concentration of (A) is not up to the standard 2 Thereby making the whole absorption tower to absorb CO 2 Has better absorption effect and improves the CO content in the flue gas 2 And (4) a trapping effect.
The purpose of the invention can be realized by the following technical scheme:
based on flue gas CO 2 The regeneration energy-saving process for purification comprises the following steps:
the method comprises the following steps: removing impurities: will contain CO 2 The flue gas is introduced into the purification cavity to remove impurities in the flue gas, and the CO after impurity removal is carried out 2 Introducing into an absorption tower;
step two: CO2 2 Absorption of (2): spraying barren solution into two absorption cavities of the absorption tower to enable the barren solution to be in countercurrent contact with the flue gas, and finishing CO 2 Absorbing to obtain a pregnant solution;
step three: CO2 2 Absorption of (2): heating the rich solution, and introducing the heated rich solution into the reactorThe gravity reactor utilizes the flowing behavior of a multi-phase flow system under the condition of supergravity to strengthen the relative speed and mutual contact between phases, thereby realizing the processes of mass and heat transfer and chemical reaction, and leading CO to be in contact with each other 2 Rapid desorption from the absorbent;
step four: separation: the desorbed regeneration gas enters a separator for separation to obtain product gas to be discharged; and introducing the desorbed barren solution into an absorption tower for secondary absorption or discharging.
As a further scheme of the invention: in the first step, the impurities in the flue gas comprise sulfur-containing and nitrate-containing gas or dust.
As a further scheme of the invention: the sulfur-containing and nitrate-containing gas in the flue gas is treated by an activated carbon fluidized bed adsorber, and the dust is treated by a dust removal filter bag.
As a further scheme of the invention: in the second step, after the absorption tower sprays the barren solution to obtain rich solution, the CO is removed 2 The flue gas is discharged from the top of the absorption tower.
As a further scheme of the invention: in the second step, the barren solution of the absorption tower absorbs CO 2 The temperature of the obtained rich solution is 40-45 ℃;
in the third step, the temperature of the rich solution after being heated is 90-95 ℃.
As a further scheme of the invention: in the second step, the absorption tower comprises a main absorption cavity and an auxiliary absorption cavity, the main absorption cavity and the auxiliary absorption cavity are communicated with each other, wherein,
the main absorption cavity and the auxiliary absorption cavity are both used for spraying barren solution to CO 2 Absorption is carried out.
As a further scheme of the invention: the main absorption cavity is used as a main working cavity and is used for spraying barren liquor to carry out CO 2 The absorption and auxiliary absorption cavity is used for absorbing the rich liquid CO in the main absorption cavity 2 The concentration is optimized.
As a further scheme of the invention: when the main absorption cavity does not work, the auxiliary absorption cavity is used as the main working cavity for spraying barren solution to carry out CO 2 And (4) absorbing.
As a further scheme of the invention: the main absorption cavity and the auxiliary absorption cavity work simultaneously and are used for spraying barren liquorCO removal 2 And (4) absorbing.
As a further scheme of the invention: the absorption tower further comprises a control system for discharging the rich liquid from the absorption tower, and CO in the rich liquid discharged from the main absorption cavity and the auxiliary absorption cavity is discharged through the control system 2 And (4) adjusting the concentration.
The invention has the beneficial effects that: the absorption tower is arranged into a whole consisting of a main absorption cavity and an auxiliary absorption cavity, and the main absorption cavity is CO under normal use 2 The main absorption cavity absorbs CO through the auxiliary absorption cavity 2 Further CO is carried out when the concentration of (A) is not up to the standard 2 Thereby making the whole absorption tower to absorb CO 2 Has better absorption effect and improves the CO content in the flue gas 2 A trapping effect;
the invention can simultaneously use the main absorption cavity and the auxiliary absorption cavity and carry out CO treatment 2 Absorbing the whole flue gas CO 2 The flue gas amount which can be processed by the capture system hypergravity regeneration energy-saving process can be greatly improved;
the invention can also use the auxiliary absorption cavity pair CO independently 2 The absorption can effectively ensure that when the main absorption cavity fails, the whole flue gas CO is absorbed 2 The capture system hypergravity regeneration energy-saving process can be effectively carried out;
according to the invention, the concentration of the barren solution discharged from the supergravity reactor is detected, so that the barren solution meeting the concentration requirement enters the absorption tower for the second time to carry out the second CO 2 The absorption of the barren solution is effectively realized, and the whole process is more energy-saving and environment-friendly.
Drawings
The invention is further described below with reference to the accompanying drawings.
FIG. 1 is a schematic view of a process flow diagram of the present invention;
FIG. 2 is a schematic view of the structure of an absorption column of the present invention.
In the figure: 1. a purification chamber; 101. a dissolution chamber; 2. an absorption tower; 201. a primary absorption cavity; 202. an auxiliary absorption cavity; 203. a ventilation duct; 204. a lean solution delivery pipe; 205. a main rich liquid conduit; 206. an auxiliary rich liquid pipeline; 207. a total rich liquor conduit; 208. a first liquid return pipeline; 209. a return air duct; 3. a hypergravity reactor; 301. a first regeneration gas conduit; 302. a liquid outlet pipeline; 303. a second liquid return pipeline; 304. a waste liquid pipe; 4. a separator; 5. a heat exchanger.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
Referring to FIGS. 1-2, the present invention is a flue gas-based CO 2 The purified regeneration energy-saving process comprises the following steps:
the method comprises the following steps: removing impurities: will contain CO 2 The flue gas is introduced into the purifying cavity 1 to remove impurities in the flue gas, and the CO after impurity removal is carried out 2 Introducing into an absorption tower 2;
step two: CO2 2 Absorption of (2): spraying barren solution into the absorption tower 2 from top to bottom, wherein the barren solution is in countercurrent contact with the flue gas to finish CO 2 Obtaining a rich solution;
step three: CO2 2 Absorption of (2): heating the rich solution, introducing the heated rich solution into a hypergravity reactor 3, and strengthening the relative speed and mutual contact between phases by utilizing the flowing behavior of a multiphase flow system under the hypergravity condition, thereby realizing the mass and heat transfer process and the chemical reaction process, so that CO can be used for the treatment of the CO 2 Rapid desorption from the absorbent;
step four: separation: the desorbed regeneration gas enters a separator 4 for separation to obtain product gas to be discharged; the desorbed lean solution is introduced into the absorption tower 2 for secondary absorption or discharged.
In the first step, the purification cavity 1 is used for carrying out desulfurization and denitrification and dust removal treatment on flue gas, the bottom of the purification cavity 1 is detachably connected with a dissolution cavity 101, and the dissolution cavity 101 is filled with aqueous solution;
specifically, the flue gas enters the purification cavity 1 through one side of the bottom of the purification cavity 1, desulfurization and denitrification are carried out through an activated carbon fluidized bed adsorber in the purification cavity 1, and dust in the flue gas is adsorbed through a dust removal filter bag;
wherein, the dust filter bag is arranged below the activated carbon fluidized bed adsorber in the purification cavity 1.
In the second step, the absorption tower 2 comprises a main absorption cavity 201 and an auxiliary absorption cavity 202, the main absorption cavity 201 is connected with the auxiliary absorption cavity 202 through a ventilation pipeline 203, lean solution delivery pipes 204 are arranged at the tops of the main absorption cavity 201 and the auxiliary absorption cavity 202, and the lean solution delivery pipes 204 respectively spray lean solutions into the main absorption cavity 201 and the auxiliary absorption cavity 202 through two branch pipelines;
a main rich liquid pipeline 205 is arranged at the bottom of the main absorption cavity 201, an auxiliary rich liquid pipeline 206 is arranged at the bottom of the auxiliary absorption cavity 202, the main rich liquid pipeline 205 is connected with a tee joint, one tee joint is connected with a total rich liquid pipeline 207, the other tee joint is connected with a first liquid return pipeline 208, an outlet of the first liquid return pipeline 208 is arranged at the top of the auxiliary absorption cavity 202, and the auxiliary rich liquid pipeline 206 is connected with the total rich liquid pipeline 207;
wherein the content of the first and second substances,
an electric control valve I is arranged on the main rich liquid pipeline 205, an electric control valve II is arranged on the auxiliary rich liquid pipeline 206, an electric control valve III and an electric control valve V are arranged on the main rich liquid pipeline 207, an electric control valve IV is arranged on the first liquid return pipeline 208, and a first liquid return pump is also arranged on the first liquid return pipeline 208;
when the absorption cavity is used, the flue gas purified by the purification cavity 1 is introduced along the bottom of the side surface of the main absorption cavity 201, and enters the auxiliary absorption cavity 202 through the air exchange pipeline 203, so that the main absorption cavity 201 and the auxiliary absorption cavity 202 are filled with the flue gas, the lean solution conveying pipe 204 sprays the lean solution into the main absorption cavity 201 or the auxiliary absorption cavity 202, and CO is treated 2 Thereby obtaining a rich liquid.
Wherein, the top of the main absorption cavity 201 and the auxiliary absorption cavity 202 are both provided with an air return pipeline 209, the other end of the air return pipeline 209 is arranged in the dissolution cavity 101, and CO is removed through the air return pipeline 209 2 The flue gas is introduced into the dissolving cavity 101 for absorption and purification.
In the third step, the rich solution discharged from the absorption tower is subjected to heat exchange treatment through a heat exchanger 5, so that the temperature of the rich solution is raised to 90-95 ℃, and the raised rich solution is introduced into a supergravity reactor 3 for desorption treatment;
wherein, a first regeneration gas pipeline 301 is arranged at the upper end of the supergravity reactor 3, the other end of the first regeneration gas pipeline 301 is connected with a separator 4, and the separator 4 is provided with an exhaust pipeline;
a liquid outlet pipeline 302 is arranged at the lower end of the supergravity reactor 3, a second liquid return pipeline 303 is arranged on the liquid outlet pipeline 302 through a three-way joint, the other end of the second liquid return pipeline 303 is connected to the lean liquid conveying pipe 204, and the other joint of the three-way joint is connected with a waste liquid pipe 304;
wherein, the second liquid return pipeline 303 is provided with an electric control valve six, and the waste liquid pipe 304 is provided with an electric control valve seven.
Example 2
In flue gas CO 2 The capture system hypergravity regeneration energy-saving process is also provided with a control system, and the control system is used for monitoring the concentration of the rich liquid discharged from the absorption tower 2;
a first concentration monitor is arranged on the main rich liquid pipeline 205, a second concentration monitor is arranged on the auxiliary rich liquid pipeline 206, and the first concentration monitor is used for discharging rich liquid CO from the main absorption cavity 201 2 Concentration monitoring instrument for assisting absorption cavity 202 to discharge rich liquid CO 2 Monitoring the concentration;
the concentration monitoring instrument I and the concentration monitoring instrument II are in system linkage with the electric regulating valve I, the electric regulating valve II, the electric regulating valve III, the electric regulating valve IV and the electric regulating valve V;
the first concentration monitor and the second concentration monitor are CO 2 A concentration monitor;
the method specifically comprises the following steps: the main absorption cavity 201 works, the auxiliary absorption cavity 202 does not work, and a concentration monitor I monitors that the rich solution discharged from the main rich solution pipeline 205 contains CO 2 The concentration value of the second monitoring auxiliary rich liquid pipeline 206 is marked as P1, and the rich liquid discharged by the second monitoring auxiliary rich liquid pipeline 206 contains CO 2 Is marked as P2, controlThe system presets rich liquid containing CO 2 Pi, the rich liquid discharge process is as follows:
s1: when the P1 is more than or equal to Pi, the electric control valve I, the electric control valve III and the electric control valve V are in an opening state, and the electric control valve II and the electric control valve IV are in a closing state, so that the rich solution flows into the hypergravity reactor 3 through the main rich solution pipeline 205 and the total rich solution pipeline 207;
s2: when P1 is less than Pi, the electric control valve I, the electric control valve II, the electric control valve III and the electric control valve IV are all in an open state, the electric control valve V is in a closed state, rich liquid discharged from the main absorption cavity 201 is introduced into the auxiliary absorption cavity 202 through the first liquid return pump for secondary spraying, the rich liquid discharged from the auxiliary absorption cavity 202 is discharged through the auxiliary rich liquid pipeline 206, and in the process of discharging the rich liquid from the auxiliary absorption cavity 202;
s21: when P2 is larger than or equal to Pi, the electric control valve I, the electric control valve II, the electric control valve IV and the electric control valve V are all in an open state, and the electric control valve III is in a closed state, so that the rich liquid discharged from the main absorption cavity 201 flows into the supergravity reactor 3 through the first liquid return pipeline 208, the auxiliary absorption cavity 202, the auxiliary rich liquid pipeline 206 and the total rich liquid pipeline 207;
s22: when P2 is less than Pi, the electric control valve I, the electric control valve II, the electric control valve III and the electric control valve IV are kept in an opening state, the electric control valve V is kept in a closing state, and the rich liquid discharged from the main absorption cavity 201 is circularly sprayed through the first liquid return pipeline 208, the auxiliary absorption cavity 202, the auxiliary rich liquid pipeline 206 and the total rich liquid pipeline 207 until P2 is more than or equal to Pi.
Example 3
The main absorption cavity 201 does not work, the auxiliary absorption cavity 202 works, and the auxiliary absorption cavity 202 has two working modes:
z1: when the rich liquid P2 discharged from the auxiliary absorption cavity 202 is less than Pi, the electric control valve II, the electric control valve III and the electric control valve IV are kept in an open state, and the electric control valve V is kept in a closed state, so that the rich liquid flows back to the auxiliary absorption cavity 202 to be sprayed for the second time until the P2 is more than or equal to Pi;
when P2 is larger than or equal to Pi, the electric control valve III and the electric control valve IV keep closed states, and the electric control valve II and the electric control valve V keep open states;
z2: the control system controls the first electric regulating valve, the third electric regulating valve and the fourth electric regulating valve to keep the closed state, and controls the second electric regulating valve and the fifth electric regulating valve to keep the open state, so as to control the rich liquid CO 2 The concentration was not monitored.
Example 4
The main absorption cavity 201 and the auxiliary absorption cavity 202 work simultaneously, and the rich liquid CO discharged from the main absorption cavity 201 and the auxiliary absorption cavity 202 2 The concentration control system does not monitor;
namely, the lean solution delivery pipe 204 sprays the lean solution into the main absorption cavity 201 and the auxiliary absorption cavity 202 through two branch pipes, so that the rich solution discharged from the main absorption cavity 201 and the rich solution discharged from the auxiliary absorption cavity 202 are converged and discharged through the main rich solution pipe 205;
the main absorption cavity 201 and the auxiliary absorption cavity 202 work simultaneously to ensure that the flue gas CO 2 The working efficiency of the hypergravity regeneration energy-saving process of the trapping system can be higher.
Example 5
The control system is also used for monitoring the concentration of the barren liquor discharged from the liquor outlet pipeline 302 of the supergravity reactor 3, and a pH monitor is arranged on the liquor outlet pipeline 302;
specifically, the pH monitor is linked with a six electric regulating valve system and a seven electric regulating valve system;
when the PH of the barren liquor discharged by the supergravity reactor 3 and obtained by a PH monitor is more than or equal to 9, the electric regulating valve six is opened, the electric regulating valve seven is closed, the barren liquor is subjected to heat exchange through the heat exchanger 5, the temperature of the barren liquor reaches 40-45 ℃, then the barren liquor is led into the barren liquor conveying pipe 204, and the barren liquor is led into the main absorption cavity 201 or the auxiliary absorption cavity 202 through the barren liquor conveying pipe 204 to carry out secondary CO 2 The absorption of (2);
when the pH of the barren liquor discharged from the supergravity reactor 3 obtained by the pH monitor is less than 9, the electric control valve six is closed, the electric control valve seven is opened, and the barren liquor is discharged through the waste liquor pipe 304.
While one embodiment of the present invention has been described in detail, the description is only a preferred embodiment of the present invention and should not be taken as limiting the scope of the invention. All equivalent changes and modifications made within the scope of the present invention shall fall within the scope of the present invention.
Claims (10)
1. Based on flue gas CO 2 The purified regeneration energy-saving process is characterized by comprising the following steps of:
the method comprises the following steps: removing impurities: will contain CO 2 The flue gas is introduced into the purification cavity (1) to remove impurities in the flue gas, and the CO after impurity removal 2 Introducing into an absorption tower (2);
step two: CO2 2 Absorption of (2): spraying barren liquor into two absorption cavities of the absorption tower (2) to enable the barren liquor to be in countercurrent contact with flue gas, and completing CO2 absorption to obtain rich liquor;
step three: CO2 2 The absorption of (2): heating the rich liquid, guiding the heated rich liquid into a hypergravity reactor (3), and strengthening the relative speed and mutual contact between phases by utilizing the flowing behavior of a multi-phase flow system under the condition of hypergravity, thereby realizing the processes of mass and heat transfer and chemical reaction, and leading CO to be in contact with each other 2 Rapid desorption from the absorbent;
step four: separation: the desorbed regeneration gas enters a separator (4) for separation to obtain product gas to be discharged; the desorbed barren solution is introduced into the absorption tower (2) for secondary absorption or discharged.
2. Flue gas based CO according to claim 1 2 The regeneration energy-saving purification process is characterized in that in the step one, impurities in the flue gas comprise sulfur-containing and nitrate-containing gas or dust.
3. Flue gas based CO according to claim 2 2 The regeneration energy-saving purification process is characterized in that sulfur-containing and nitrate-containing gas in the flue gas is treated by an activated carbon fluidized bed adsorber, and dust is treated by a dust removal filter bag.
4. Flue gas based CO according to claim 1 2 The regeneration energy-saving process of purification is characterized in that the step twoIn the middle, after the absorption tower (2) sprays the barren solution to obtain rich solution, the CO is removed 2 The flue gas is discharged from the top of the absorption tower (2).
5. Flue gas based CO according to claim 1 2 The regeneration energy-saving process for purification is characterized in that in the second step, the barren solution of the absorption tower (2) absorbs CO 2 The temperature of the obtained rich solution is 40-45 ℃;
in the third step, the temperature of the rich solution after being heated is 90-95 ℃.
6. Flue gas based CO according to claim 1 2 The regeneration energy-saving process for purification is characterized in that in the second step, the absorption tower (2) comprises a main absorption cavity (201) and an auxiliary absorption cavity (202), the main absorption cavity (201) is communicated with the auxiliary absorption cavity (202),
the main absorption cavity (201) and the auxiliary absorption cavity (202) are used for spraying lean solution to absorb CO 2.
7. Flue gas based CO according to claim 6 2 The regeneration energy-saving purification process is characterized in that a main absorption cavity (201) is used as a main working cavity and used for spraying lean solution to absorb CO2, and an auxiliary absorption cavity (202) is used for optimizing the concentration of rich solution CO2 in the main absorption cavity (201).
8. Flue gas based CO according to claim 6 2 The regeneration energy-saving process for purification is characterized in that when the main absorption cavity (201) does not work, the auxiliary absorption cavity (202) serves as a main working cavity and is used for spraying lean solution to absorb CO 2.
9. Flue gas based CO according to claim 6 2 The regeneration energy-saving process for purification is characterized in that the main absorption cavity (201) and the auxiliary absorption cavity (202) work simultaneously and are used for spraying lean solution to absorb CO 2.
10.Flue gas based CO according to any one of claims 7-9 2 The purified regeneration energy-saving process is characterized by also comprising a control system for discharging rich liquid from the absorption tower (2), wherein the control system is used for finishing the discharge of CO in the rich liquid from the main absorption cavity (201) and the auxiliary absorption cavity (202) 2 And (4) adjusting the concentration.
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