CN111203026A - Purification and recovery method suitable for amine liquid - Google Patents
Purification and recovery method suitable for amine liquid Download PDFInfo
- Publication number
- CN111203026A CN111203026A CN202010060778.7A CN202010060778A CN111203026A CN 111203026 A CN111203026 A CN 111203026A CN 202010060778 A CN202010060778 A CN 202010060778A CN 111203026 A CN111203026 A CN 111203026A
- Authority
- CN
- China
- Prior art keywords
- amine liquid
- resin exchanger
- exchanger
- compressed air
- anion
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D36/00—Filter circuits or combinations of filters with other separating devices
Abstract
The invention provides a purification and recovery method suitable for amine liquid, which can remove oil stains and metal cation pollution in the amine liquid, can reduce the carrying amount of desalted water in the recovery process of the amine liquid, and reduces the purification cost of the amine liquid, and the purification and recovery method comprises the following steps: s1: purifying the amine liquid, namely sequentially passing the amine liquid through a leather glue fiber filter, an activated carbon filter, an impurity removal filter, a chelating resin exchanger and an anion resin exchanger to remove oil stains, colored macromolecules, impurities, cation pollution and acid anions in the amine liquid; s2: and (4) recovering the amine liquid, closing all valves before the chelating resin exchanger after S1 is finished, injecting compressed air into the chelating resin exchanger and the anion resin exchanger, and then soaking and recovering by using desalted water.
Description
Technical Field
The invention relates to the field of amine liquid purification, in particular to a purification and recovery method suitable for amine liquid.
Background
Due to long-term operation of the desulfurization and decarburization amine liquid system, degradation products and corrosion products in the system are accumulated continuously. Among them, salts produced by the reaction of organic amine cations and acidic anions, such as formate, acetate, sulfate, hydrochloride, oxalate, etc., which cannot be regenerated by heating, are collectively called thermal stable salts (abbreviated as HSS). The anion of the thermal stable salt is combined with amine, solvent amine can not be recovered by a regeneration method, so that the solvent amine with the same mole number as that of the thermal stable salt is fixed and can not be effectively utilized, the absorption amount of acid gas is reduced along with the increase of the running time, and the reduction of the absorption capacity needs to be compensated by continuously supplementing fresh solvent. Meanwhile, the corrosivity of the solvent is enhanced due to the accumulation of the heat stable salt, so that amine liquid is easy to foam, and the operation stability of the device is affected. Therefore, in order to ensure the safe and stable operation of the device, slow down the corrosion of equipment, reduce impurities in the amine liquid and improve the absorption amount of the acid gas by the amine liquid, the purification of the amine liquid is imperative.
In terms of the technology and the actual situation mastered at present, the anion exchange technology is the most widely, economically and practically applicable technology for removing the heat stable salt. The most applied at present is the anion exchange process, which has the advantages of simple equipment, less investment, high efficiency, simple operation and the like, but the process can not remove the pollution of metal cations (such as iron, copper, calcium ions and the like) in amine liquid and oil pollution, and the process adopts 4-8% of sodium hydroxide solution to regenerate anion resin, a large amount of waste alkali liquid is discharged into a sewage treatment system of a factory, and the impact on the sewage treatment system is larger.
In addition, in the process of using the amine liquid purification device, after the heat stable salt of the unpurified amine liquid is removed by the resin, part of the amine liquid is adhered to the resin and remains in the resin and the tank, and in order to recover the part of the amine liquid, the most commonly adopted method is to wash and recover the part of the amine liquid by desalted water. This results in a large amount of desalted water entering the amine system, not only reducing the amine liquor concentration, but also requiring a large investment cost to concentrate.
Disclosure of Invention
The invention aims to provide a purification and recovery method suitable for amine liquid, which can remove oil stains and metal cation pollution, colored macromolecules, mechanical impurities and acid anions in the amine liquid, reduce the carrying amount of desalted water in the recovery process of the amine liquid and reduce the purification cost of the amine liquid.
The embodiment of the invention is realized by the following steps:
a purification and recovery method suitable for amine liquid comprises the following steps:
s1: purifying the amine liquid, namely sequentially passing the amine liquid through a leather glue fiber filter, an activated carbon filter, an impurity removal filter, a chelating resin exchanger and an anion resin exchanger to remove oil stains, colored macromolecules, mechanical impurities, metal cations and acid anions in the amine liquid;
s2: and (4) recovering the amine liquid, closing all valves before the chelating resin exchanger after S1 is finished, injecting compressed air into the chelating resin exchanger and the anion resin exchanger, and then soaking and recovering by using desalted water.
In the preferred embodiment of the present invention, the specific operation of S1 is as follows:
s11: amine liquid enters from an amine liquid input end of the rubber fiber filter, and a small amount of oil stains dissolved in the amine liquid are removed by adsorption;
s12: the amine liquid without oil stain enters an activated carbon filter to remove colored macromolecules in the amine liquid;
s13: the amine liquid with the colored macromolecules removed enters an impurity removal filter, and the impurity removal filter removes mechanical impurities in the amine liquid through precise filtration;
s14: the amine liquid without mechanical impurities enters a chelating resin exchanger to remove metal cation pollution in the amine liquid, wherein the cation pollution comprises iron ions, copper ions and calcium ions;
s15: and (4) the amine solution without metal cation pollution enters an anion resin exchanger to remove acid anions in the amine solution.
In a preferred embodiment of the present invention, the activated carbon in the activated carbon filter is prepared by high-temperature calcination of a wood particle activated carbon loaded catalyst.
In the preferred embodiment of the present invention, the high temperature calcination is performed at a high temperature of 400-600 ℃ under the protection of inert gas.
In a preferred embodiment of the present invention, the catalyst comprises one or more of metallic nickel, metallic palladium, metallic nickel oxide and metallic palladium oxide.
In a preferred embodiment of the present invention, the filtration precision of the impurity removing filter in S13 is 0.1 μm.
In the preferred embodiment of the present invention, the specific operation of S2 is as follows:
s21: pressurizing and recovering, injecting compressed air into the chelating resin exchanger and the anion resin exchanger, and opening an amine liquid output end of the anion resin exchanger to discharge amine liquid when the pressure in the anion resin exchanger reaches a set value;
s22: secondary pressurization recovery, when the pressure in the chelating resin exchanger is lower than a set value, closing the amine liquid output end, and repeating S21;
s23: soaking and recovering desalted water, namely injecting the desalted water into a chelating resin exchanger to soak resin, then injecting compressed air into the chelating resin exchanger to pressurize, and closing a compressed air valve to release the desalted water to an anion resin exchanger when the pressure reaches a set value;
s24: like S23, the desalted water is injected into the anion resin exchanger to soak the resin, and then compressed air is injected into the anion resin exchanger; and when the pressure value in the anion resin exchanger reaches a set value, closing the compressed air and opening the amine liquid output end of the anion resin exchanger until the pressure of the anion resin exchanger is lower than the set value, and closing all the valves.
In a preferred embodiment of the present invention, the specific operations of S21 include: and S1, closing all valves in front of the chelating resin exchanger, opening compressed air, enabling the compressed air to enter the anion resin exchanger through the chelating resin exchanger, closing a compressed air input end of the chelating resin exchanger when the pressure value in the anion resin exchanger reaches a set value, and opening an amine liquid output end of the anion resin exchanger to discharge the amine liquid.
In a preferred embodiment of the present invention, the specific operations of S23 are: when the pressure in the chelating resin exchanger is lower than a set value, closing the output end of the chelating resin exchanger to ensure that desalted water only enters the chelating resin exchanger; when the desalted water is fed to submerge the resin, closing a desalted water inlet valve; injecting compressed air into the chelating resin exchanger; when the pressure value in the chelating resin exchanger reaches a set value, the compressed air is closed, the amine liquid output end of the chelating resin exchanger is opened, and desalted water enters the anion resin exchanger.
In a preferred embodiment of the present invention, the setting value is 300Kpa, the setting value is 30Kpa, and the time for soaking the resin is equal to or greater than 5 min.
The embodiment of the invention has the beneficial effects that: the invention provides a method for purifying and recovering amine liquid, which takes an active carbon filter, a chelating resin exchanger and an anion resin exchanger as centers, and simultaneously combines a submicron impurity removal filter and a leather viscose fiber filter as an assistant, so that oil stains, colored macromolecules, metal cations and acid anions in an alcohol amine solution can be removed, the carrying amount of desalted water in the process of recovering the amine liquid can be reduced, and the once soaking recovery rate is up to 92 percent.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some embodiments of the present invention and therefore should not be considered as limiting the scope, and for those skilled in the art, other related drawings can be obtained according to the drawings without inventive efforts.
FIG. 1 is a diagram of an amine liquid purification skid-mounted system according to an embodiment of the invention;
icon: 001-hide glue fiber filter; 002-activated carbon filter; 003-impurity removal filter; 004-chelating resin exchanger; 005-anion resin exchanger; 006-acid liquid pump; 007-lye pump.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, 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 some, but not all, embodiments of the present invention. The components of embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations.
Thus, the following detailed description of the embodiments of the present invention, presented in the figures, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. 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.
It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, it need not be further defined and explained in subsequent figures.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings or the orientations or positional relationships that the products of the present invention are conventionally placed in use, and are only used for convenience in describing the present invention and simplifying the description, but do not indicate or imply that the devices or elements referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," "third," and the like are used solely to distinguish one from another and are not to be construed as indicating or implying relative importance.
Furthermore, the terms "horizontal", "vertical", "overhang" and the like do not imply that the components are required to be absolutely horizontal or overhang, but may be slightly inclined. For example, "horizontal" merely means that the direction is more horizontal than "vertical" and does not mean that the structure must be perfectly horizontal, but may be slightly inclined.
In the description of the present invention, it should also be noted that, unless otherwise explicitly specified or limited, the terms "disposed," "mounted," "connected," and "connected" are to be construed broadly and may, for example, be fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
First embodiment
In the prior art, the amine desulphurization and decarbonization device generally has the problem of accumulation of heat stable salt in amine liquid, and when the content of the heat stable salt in the amine liquid is accumulated to a certain amount, a series of problems can be caused, such as darkening of color, increase of viscosity, foaming of solution, low acid gas load, enhancement of corrosivity of the amine liquid and the like.
Please refer to fig. 1, which includes a leather-rubber fiber filter 001, an activated carbon filter 002, an impurity removal filter 003, a chelate resin exchanger 004, and an anion resin exchanger 005, wherein an amine liquid output end of the leather-rubber fiber filter 001 is connected to an amine liquid input end of the activated carbon filter 002, an amine liquid output end of the activated carbon filter 002 is connected to an amine liquid input end of the impurity removal filter 003, an amine liquid output end of the impurity removal filter 003 is connected to an input end of the chelate resin exchanger 004, and an output end of the chelate resin exchanger 004 is connected to an input end of the anion resin exchanger 005.
More specifically, the amine liquid purification skid-mounted system in this embodiment further includes an acid liquid pump 006 and an alkaline liquid pump 007, the chelate resin exchanger 004 is provided with an acid liquid input end, and the regenerated acid liquid enters the chelate resin exchanger 004 through the acid liquid pump 006; the anion resin exchanger 005 is also provided with an alkali liquor input end, and regenerated alkali liquor enters the anion resin exchanger 005 through the alkali liquor pump 007. The hide glue fiber filter 001, the chelating resin exchanger 004 and the anion resin exchanger 005 are also provided with a compressed air input. The chelating resin exchanger 004 is also provided with a desalted water input end.
More specifically, both the chelate resin exchanger 004 and the anion resin exchanger 005 in the present embodiment are provided with wastewater output ends, each of which is connected to an acid-base neutralization buffer tank connected to a sewage treatment tank. The anion resin exchanger 005 is provided with an amine liquid output terminal connected to an underground tank.
The leather glue fiber filter 001 of the amine liquid purification skid-mounted system in the embodiment is a leather glue fiber adsorption tank, the activated carbon filter 002 is a special activated carbon adsorption tank, the impurity removal filter 003 adopts a precision mechanical filter, the chelate resin exchanger 004 is a chelate resin adsorption tank, the anion resin exchanger 005 is an anion exchange resin tank, and all the tank bodies are connected in sequence and all adopt an up-in-down mode. And is externally connected with a desalted water pipeline, an alkaline liquid pipeline, an acid liquid pipeline, an air pipeline, a purifying liquid pipeline and a waste liquid pipeline. The acid liquor pipeline is connected with the chelating resin tank, the alkaline liquor pipeline is connected with the anion exchange resin tank, and the desalination water pipeline and the air pipeline are connected with the chelating resin tank and the anion exchange resin tank.
More specifically, the amine liquid purification skid-mounted method in this embodiment includes the following steps:
s1: purifying, namely removing oil stains, colored macromolecules, mechanical impurities, metal cations and acid anions in the amine solution sequentially through a leather-rubber fiber filter 001, an activated carbon filter 002, an impurity removal filter 003, a chelate resin exchanger 004 and an anion resin exchanger 005;
s2: after the recovery and purification steps are finished, all valves in front of the chelate resin exchanger 004 are closed, compressed air is injected into the chelate resin exchanger 004 and the anion resin exchanger 005, and then desalted water is used for soaking and recovery;
s3: regenerating resin, namely opening exhaust valves at the tops of the chelate resin exchanger 004 and the anion resin exchanger 005, respectively injecting regenerated acid liquid into the chelate resin exchanger 004, injecting regenerated alkali liquid into the anion resin exchanger 005, and cleaning the resin by using desalted water after treatment;
s4: repeating S1-S3.
More specifically, S1 in this embodiment specifically operates as follows:
s11: amine liquid enters from an amine liquid input end of the leather-rubber fiber filter 001, and a small amount of oil stains dissolved in the amine liquid are removed by adsorption; the amine liquid passes through an adsorption tank made of the collagen fibers, oil stains in the amine liquid are adsorbed, and the collagen fibers are non-polar adsorbed, so that the amine liquid can be swept by air and recycled, and the cost is low;
s12: the amine liquid without oil stain enters an active carbon filter 002 to remove colored macromolecules in the amine liquid; the activated carbon in the activated carbon filter 002 is prepared by loading wood particle activated carbon with a catalyst and calcining at high temperature; more specifically, under the protection of inert gas, activated carbon is loaded with metal nickel and metal palladium or oxides thereof at a high temperature of 400-600 ℃ and calcined at a high temperature, so that colored macromolecules in amine liquid can be effectively removed;
s13: the amine liquid without colored macromolecules enters an impurity removal filter 003, the impurity removal filter 003 is used for precisely filtering and removing mechanical impurities in the amine liquid through a high-precision precise impurity removal filter 003, and the filtering precision of the impurity removal filter 003 is 0.1 mu m;
s14: the amine liquid without mechanical impurities enters a chelating resin exchanger 004 to remove metal cation pollution in the amine liquid, wherein the cation pollution comprises iron ions, copper ions, calcium ions and the like;
s15: the amine solution without metal cation pollution enters an anion resin exchanger 005 to remove acid anions in the amine solution.
In the process of using the amine liquid purification device, when the resin needs to be regenerated, part of the amine liquid is adhered to the resin and remains in the resin tank, and in order to recover the part of the amine liquid, the most of the amine liquid is recovered by flushing with desalted water at present. This results in a large amount of desalted water entering the amine system, not only reducing the amine liquor concentration, but also requiring a large investment cost to concentrate. The invention adopts the compressed air pressurization recovery and the desalted water soaking recovery process, thereby not only reducing the carrying amount of desalted water, but also achieving the once soaking recovery rate as high as 92 percent. The implementation steps are as follows:
s21: pressurizing and recovering, closing all valves in front of the chelate resin exchanger 004 after S1 is finished, opening compressed air, enabling the compressed air to enter the anion resin exchanger 005 through the chelate resin exchanger 004, closing a compressed air input end of the chelate resin exchanger 004 when the pressure value in the anion resin exchanger 005 reaches a set value of 300Kpa, and opening an amine liquid output end of the anion resin exchanger 005 to discharge amine liquid;
s22: performing secondary pressurization recovery, closing an amine liquid output end when the pressure in the chelate resin exchanger 004 is lower than a set value of 30Kpa, repeating S21, opening compressed air, pressurizing and discharging;
s23: soaking and recovering desalted water, and when the pressure in the chelate resin exchanger 004 is lower than a set value of 30Kpa, closing the amine liquid output end of the chelate resin exchanger 004 to ensure that the desalted water only enters the chelate resin exchanger 004; closing a water inlet valve of the desalted water when the inlet water of the desalted water just exceeds the resin, and soaking for 5 min; then injecting compressed air into the chelate resin exchanger 004; when the pressure value in the chelate resin exchanger 004 reaches 300Kpa, the compressed air is closed, the amine liquid output end of the chelate resin exchanger 004 is opened, and desalted water enters the anion resin exchanger 005;
s24: after the anion resin exchanger 005 is soaked in desalted water for 5min, compressed air is injected into the anion resin exchanger 005; when the pressure value in the anion resin exchanger 005 reaches 300kpa, the compressed air is closed; and opening the amine liquid output end of the anion resin exchanger 005 to output the amine liquid, closing all valves after the pressure of the anion resin exchanger 005 is lower than 30Kpa, and finishing the amine liquid purification and recovery step.
More specifically, the specific operation of S3 in this embodiment is as follows:
s31: feeding a regeneration liquid: opening exhaust valves at the tops of the chelate resin exchanger 004 and the anion resin exchanger 005, opening an acid liquid pump 006 and an alkali liquid pump 007, respectively injecting regenerated acid liquid and regenerated alkali liquid into the chelate resin exchanger 004 and the anion resin exchanger 005, wherein the regenerated acid liquid and the regenerated alkali liquid both submerge the resins in the chelate resin exchanger 004 and the anion resin exchanger 005, then respectively opening wastewater output ends in the chelate resin exchanger 004 and the anion resin exchanger 005, and the waste acid and the waste alkali liquid flow into an external neutralization buffer tank and then are discharged into a sewage treatment tank;
s32: purging with alkali liquor, closing valves of all the chelating resin exchangers 004 and the anion resin exchanger 005 after the regeneration liquid enters, and pressurizing and purging the regeneration liquid;
s33: cleaning, namely soaking and cleaning the resin by using desalted water;
s34: the resin is washed by soaking with desalted water repeatedly.
Repeating the steps, and entering the next period after one period of amine liquid purification is finished.
In summary, the present embodiment uses the activated carbon filter, the chelating resin exchanger and the anion resin exchanger as the center, and combines the submicron impurity removal filter and the leather viscose fiber filter as the auxiliary amine liquid purification skid-mounted device, which can remove the oil stain, the colored macromolecules, the metal cations and the acid anions in the alcohol amine solution, and can also reduce the carrying amount of the desalted water in the amine liquid recovery process, and the once soaking recovery rate is as high as 92%.
This description describes examples of embodiments of the invention, and is not intended to illustrate and describe all possible forms of the invention. It should be understood that the embodiments described in this specification can be implemented in many alternative forms. The figures are not necessarily to scale; some features may be exaggerated or minimized to show details of particular components. Specific structural and functional details disclosed are not to be interpreted as limiting, but merely as a representative basis for teaching one skilled in the art to variously employ the present invention. It will be appreciated by persons skilled in the art that a plurality of features illustrated and described with reference to any one of the figures may be combined with features illustrated in one or more other figures to form embodiments which are not explicitly illustrated or described. The described combination of features provides a representative embodiment for a typical application. However, various combinations and modifications of the features consistent with the teachings of the present invention may be used as desired for particular applications or implementations.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A purification and recovery method suitable for amine liquid is characterized by comprising the following steps:
s1: purifying the amine liquid, namely sequentially passing the amine liquid through a leather glue fiber filter, an activated carbon filter, an impurity removal filter, a chelating resin exchanger and an anion resin exchanger to remove oil stains, colored macromolecules, mechanical impurities, metal cations and acid anions in the amine liquid;
s2: and (4) recovering the amine liquid, closing all valves before the chelating resin exchanger after S1 is finished, injecting compressed air into the chelating resin exchanger and the anion resin exchanger, and then soaking and recovering by using desalted water.
2. The purification and recovery method for amine liquid according to claim 1, wherein the specific operation of S1 is as follows:
s11: amine liquid enters from an amine liquid input end of the leather-rubber fiber filter and is adsorbed to remove a small amount of oil stains dissolved in the amine liquid;
s12: the amine liquid without oil stain enters the activated carbon filter to remove colored macromolecules in the amine liquid;
s13: the amine liquid with the colored macromolecules removed enters the impurity removal filter, and the impurity removal filter removes mechanical impurities in the amine liquid through precise filtration;
s14: the amine liquid without mechanical impurities enters the chelating resin exchanger to remove metal cation pollution in the amine liquid, wherein the cation pollution comprises iron ions, copper ions and calcium ions;
s15: and the amine liquid from which the metal cations are removed enters the anion resin exchanger to remove the acid anions in the amine liquid.
3. The method for purifying and recovering amine liquid as claimed in claim 2, wherein the activated carbon in the activated carbon filter is prepared by high-temperature calcination of a wood particle activated carbon loaded catalyst.
4. The purification and recovery method for amine liquid as claimed in claim 3, wherein the high temperature calcination is performed at 400-600 ℃ under the protection of inert gas.
5. The method for purifying and recovering amine liquid according to claim 2, wherein the catalyst comprises one or more of metallic nickel, metallic palladium, metallic nickel oxide and metallic palladium oxide.
6. The purification and recovery method for amine liquid according to claim 2, wherein the filtration precision of the impurity removing filter in S13 is 0.1 μm.
7. The purification and recovery method for amine liquid according to claim 1, wherein the specific operation of S2 is as follows:
s21: pressurizing and recovering, injecting compressed air into the chelating resin exchanger and the anion resin exchanger, and opening an amine liquid output end of the anion resin exchanger to discharge amine liquid when the pressure in the anion resin exchanger reaches a set value;
s22: secondary pressurization recovery, when the pressure in the chelating resin exchanger is lower than a set value, the amine liquid output end is closed, and S21 is repeated;
s23: soaking and recovering desalted water, namely injecting desalted water into the chelating resin exchanger to soak resin, then injecting compressed air into the chelating resin exchanger to pressurize, and closing a compressed air valve to release desalted water to the anion resin exchanger when the pressure reaches a set value;
s24: as in S23, injecting desalted water into the anion resin exchanger to soak the resin, and then injecting compressed air into the anion resin exchanger; and when the pressure value in the anion resin exchanger reaches a set value, closing the compressed air and opening the amine liquid output end of the anion resin exchanger until the pressure of the anion resin exchanger is lower than the set value, and closing all valves.
8. The purification and recovery method for amine liquid according to claim 1, wherein the specific operation of S21 comprises: and S1, closing all valves in front of the chelating resin exchanger, opening compressed air, enabling the compressed air to enter the anion resin exchanger through the chelating resin exchanger, closing a compressed air input end of the chelating resin exchanger when the pressure value in the anion resin exchanger reaches a set value, and opening an amine liquid output end of the anion resin exchanger to discharge amine liquid.
9. The purification and recovery method for amine liquid according to claim 1, wherein the specific operations of S23 are as follows: when the pressure in the chelating resin exchanger is lower than a set value, closing the output end of the chelating resin exchanger to ensure that desalted water only enters the chelating resin exchanger; closing a water inlet valve of the desalted water when the desalted water is fed to the resin; injecting compressed air into the chelating resin exchanger; and when the pressure value in the chelating resin exchanger reaches a set value, closing the compressed air, and opening the amine liquid output end of the chelating resin exchanger to enable desalted water to enter the anion resin exchanger.
10. The method for purifying and recovering amine liquid according to claim 7, wherein the set value is 300Kpa, the set value is 30Kpa, and the time for soaking the resin is equal to or more than 5 min.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010060778.7A CN111203026A (en) | 2020-01-19 | 2020-01-19 | Purification and recovery method suitable for amine liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010060778.7A CN111203026A (en) | 2020-01-19 | 2020-01-19 | Purification and recovery method suitable for amine liquid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111203026A true CN111203026A (en) | 2020-05-29 |
Family
ID=70780914
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010060778.7A Pending CN111203026A (en) | 2020-01-19 | 2020-01-19 | Purification and recovery method suitable for amine liquid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111203026A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111701397A (en) * | 2020-07-03 | 2020-09-25 | 攀钢集团攀枝花钢铁研究院有限公司 | Process for removing sulfate ions and chloride ions in organic amine desulfurization solution and reducing loss of organic amine solution |
| CN112591927A (en) * | 2020-10-23 | 2021-04-02 | 中石化南京化工研究院有限公司 | Method for purifying and recycling desulfurized amine liquid |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU975583A1 (en) * | 1980-06-30 | 1982-11-23 | Кировский Политехнический Институт | Process for purifying effluents containing ammonia and ethylene diamine |
| CN111056671A (en) * | 2020-01-17 | 2020-04-24 | 成都能净科技有限公司 | Amine liquid purification skid-mounted system and method thereof |
-
2020
- 2020-01-19 CN CN202010060778.7A patent/CN111203026A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU975583A1 (en) * | 1980-06-30 | 1982-11-23 | Кировский Политехнический Институт | Process for purifying effluents containing ammonia and ethylene diamine |
| CN111056671A (en) * | 2020-01-17 | 2020-04-24 | 成都能净科技有限公司 | Amine liquid purification skid-mounted system and method thereof |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111701397A (en) * | 2020-07-03 | 2020-09-25 | 攀钢集团攀枝花钢铁研究院有限公司 | Process for removing sulfate ions and chloride ions in organic amine desulfurization solution and reducing loss of organic amine solution |
| CN112591927A (en) * | 2020-10-23 | 2021-04-02 | 中石化南京化工研究院有限公司 | Method for purifying and recycling desulfurized amine liquid |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101337707B (en) | Method for processing dimethylamine waste water by ion-exchange method | |
| JP4001554B2 (en) | Coke oven gas purification method | |
| CN111203026A (en) | Purification and recovery method suitable for amine liquid | |
| CN101502742A (en) | Method for removing thermostable salt in amine liquid for desulphurization | |
| CN104129831B (en) | Method for simultaneous removal and recovery of heavy metal ions and organic acid by using chelating resin | |
| CA3032534C (en) | Exhaust gas treatment device and co2 recovery device using same | |
| CN212864355U (en) | Waste acid liquid regeneration pretreatment system | |
| CN100333823C (en) | Method for purifying deterioration amine liquid using highly basic anion exchange resin | |
| CN212375042U (en) | Amine liquid purifies sled dress system | |
| CN111056671A (en) | Amine liquid purification skid-mounted system and method thereof | |
| CN106178591B (en) | A method of purification organic amine | |
| CN106422675A (en) | Purification device and purification method of organic amine desulfurizing agent in organic amine method desulfurizing process | |
| CN104193034B (en) | A kind of amine purification processes system | |
| WO2018049915A1 (en) | Cobalt complex recycling method for cobalt ammonia absorbent for simultaneous flue gas desulfurization and denitrification | |
| CN103331079A (en) | Membrane method ammonia gas treatment recovering apparatus and technology thereof | |
| CN109929998A (en) | A kind of regeneration method of copper-molybdenum saturated resin | |
| CN203090758U (en) | Filtering and reactivation device for skid-mounted natural gas desulfurized amine solution | |
| KR102570569B1 (en) | recycling apparatus and method of waste sulfuric acid | |
| CN212127781U (en) | Nickel recovery device for waste battery wastewater | |
| TWI399360B (en) | Recovery equipment for tetramethylammonium hydroxide and its method | |
| CN102815819A (en) | Low loss desulfurization solution purification process | |
| CN210044942U (en) | Amine liquid purification integrated device | |
| CN106423308B (en) | In a kind of production of Lyocell fiber in NMMO solvent recovery process cation exchange resin recovery technique | |
| CN115990394B (en) | Desalination and sodium removal system and method in ionic liquid desulfurization | |
| EP2653210A1 (en) | Combustion assembly with flue gas washing and CO2 removal and method for operating same |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20200529 |
|
| RJ01 | Rejection of invention patent application after publication |