CN113304737B - Desorption process after adsorption saturation of adsorbent - Google Patents
Desorption process after adsorption saturation of adsorbent Download PDFInfo
- Publication number
- CN113304737B CN113304737B CN202110616745.0A CN202110616745A CN113304737B CN 113304737 B CN113304737 B CN 113304737B CN 202110616745 A CN202110616745 A CN 202110616745A CN 113304737 B CN113304737 B CN 113304737B
- Authority
- CN
- China
- Prior art keywords
- adsorbent
- reactor
- adsorption saturation
- desorption
- gas
- 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.)
- Active
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/345—Regenerating or reactivating using a particular desorbing compound or mixture
- B01J20/3458—Regenerating or reactivating using a particular desorbing compound or mixture in the gas phase
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/345—Regenerating or reactivating using a particular desorbing compound or mixture
- B01J20/3458—Regenerating or reactivating using a particular desorbing compound or mixture in the gas phase
- B01J20/3466—Regenerating or reactivating using a particular desorbing compound or mixture in the gas phase with steam
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/3491—Regenerating or reactivating by pressure treatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/281—Treatment of water, waste water, or sewage by sorption using inorganic sorbents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/16—Regeneration of sorbents, filters
Landscapes
- Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Inorganic Chemistry (AREA)
- Water Treatment By Sorption (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
Abstract
The invention discloses a desorption process after adsorption saturation of an adsorbent, which comprises the following steps of S1, washing the adsorbent after adsorption saturation in organic wastewater with clear water; step S2, air purging the adsorbent surface liquid; s3, placing the adsorbent into a reactor, introducing gas into the reactor to pressurize the adsorbent, and stopping; step S4, hot steam is introduced into the reactor; step S5, continuously introducing waste heat steam while discharging the gas in the reactor; and S6, after the desorption is finished, discharging condensed water, wherein the desorption process after the adsorption saturation of the adsorbent comprises the following steps of. The desorption process after the adsorption saturation of the adsorbent disclosed by the invention enables the organic matters adsorbed in the adsorbent to be rapidly transferred to an external gas phase or a liquid phase through the internal and external desorption forces of gas and steam, and after the adsorbent reaches the adsorption capacity limit, the desorption efficiency is excellent by adopting the internal gas expansion and the external steam heating.
Description
Technical Field
The invention relates to the technical field of wastewater treatment and alumina mother liquor organic matter separation, in particular to a desorption process after adsorption saturation of an adsorbent.
Background
The organic matters in the wastewater are generally represented by using COD (Chemical Oxygen Demand chemical oxygen demand) or TOC (Total Organic Carbon total organic matter carbon) as indexes, so that the separation of organic matters in mother liquor in the alumina industry is a difficult problem at home and abroad at present, and the main stream organic matter wastewater treatment process at home and abroad adopts biological oxidation or chemical oxidation process.
In practical applications, these processes have many constraints: firstly, under the conditions of high salinity and biotoxicity, the biological oxidation process is difficult to implement; secondly, the chemical oxidation process is a chemical entropy reduction process, corresponding energy consumption is necessarily required in the treatment process, meanwhile, oxidation reduction process is carried out on organic matters and organic matters dispersed in wastewater or organic matter feed liquid, the energy utilization rate is low, and corresponding harsh oxidation conditions are required. Therefore, even if the chemical oxidation process effectively degrades the organic matters in the wastewater or the organic matter feed liquid, the engineering investment and the operation cost are high, and the two processes have a plurality of defects, so that the wide application is difficult.
Along with the increasing requirements of domestic and foreign environmental management, how to overcome the defects of the existing main flow process becomes a great difficulty of the current wastewater treatment process.
Disclosure of Invention
In order to solve the above technical problems, it is desirable to provide a desorption process after adsorption saturation of an adsorbent, which uses two desorption forces of internal gas expansion and external steam heating to improve the desorption effect of the adsorbent. The method comprises the following steps: step S1, washing the adsorbent clean water after adsorption saturation in organic wastewater;
step S2, air purging the adsorbent surface liquid;
s3, placing the adsorbent into a reactor, introducing gas into the reactor to pressurize the adsorbent, and stopping;
step S4, hot steam is introduced into the reactor;
step S5, continuously introducing waste heat steam while discharging the gas in the reactor;
and S6, after the desorption is finished, discharging condensed water.
Preferably, the method further comprises step S21, wherein after the liquid on the surface of the adsorbent is purged by air, the adsorbent is firstly placed at normal temperature for cooling.
Preferably, the method further comprises step S31 of adding an inorganic foaming agent or a liquid-phase foaming agent after the adsorbent is placed in the reactor.
Preferably, the inorganic foaming agent is an inorganic foaming agent solution.
Preferably, in step S3, the pressure of the adsorbent pressurized in the reactor is maintained for a preset period of time.
Preferably, in the step S3, a preset period of time for pressurizing the adsorbent by introducing gas into the reactor is 10-20min, and the pressure of the introduced gas is 0.4-2.0MPa.
Preferably, in step S3, the temperature of the adsorbent vapor in the reactor is gradually increased to a preset temperature.
Preferably, in the step S5, the time of continuously introducing the waste heat steam is 25-35min.
Preferably, the adsorbent is activated carbon or aluminum-silicon porous inorganic material.
The desorption process after the adsorption saturation of the adsorbent provided by the embodiment of the invention ensures that the organic matters adsorbed in the adsorbent are rapidly transferred to an external gas phase or a liquid phase through the internal and external desorption forces of gas and steam, and the desorption efficiency is excellent by adopting the internal gas expansion and the external steam heating after the adsorbent reaches the adsorption capacity limit; compared with the traditional organic wastewater adsorption and desorption process, the method has remarkable advantages in engineering investment and running cost entropy, meanwhile, unattended operation can be achieved, and the degree of automation is extremely high.
Drawings
Fig. 1 is a flow chart of a desorption process after the adsorption saturation of the adsorbent provided by the invention.
Detailed Description
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, 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 apparent that the described embodiments are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
In the adsorption process, most of organic matters in wastewater or mother liquor of alumina industry are nonpolar organic matters, under the standard condition, the organic matters can be adsorbed by the adsorbent, water and other inorganic salts belong to polar compounds which are not adsorbed by the adsorbent, during the adsorption process, the organic matters in the wastewater are continuously adsorbed by the adsorbent, and the organic matter load in the wastewater is continuously reduced until the adsorbent is close to saturation under the standard condition. The invention provides a desorption process for an adsorbent after adsorption saturation. Referring to fig. 1, a flow chart of a desorption process after the adsorption saturation of the adsorbent provided by the invention is shown. The desorption process after the adsorption saturation of the adsorbent comprises the following steps:
and S1, washing the adsorbent clean water after adsorption saturation in the organic wastewater. The primary effect of the outer surface washing treatment of the adsorbent is to reduce the surface fouling adhesion of the adsorbent.
And S2, utilizing a high-pressure air blower to blow the liquid on the surface of the adsorbent, and drying the outer surface of the adsorbent, so that the attached moisture on the outer surface can be reduced. After the liquid on the surface of the adsorbent is purged by air, the adsorbent is firstly placed at normal temperature for cooling, so that the temperature of the adsorbent reaches the normal temperature.
And S3, placing the adsorbent into a reactor, adding an inorganic foaming agent or a liquid-phase foaming agent into the reactor, introducing gas into the reactor, pressurizing the adsorbent, and stopping. Specifically, the pressure of the adsorbent in the reactor is maintained for a preset time period, the preset time period is 10-20min, the pressure of the gas introduced into the reactor is 0.4-2.0Mpa, and preferably, the pressure of the gas introduced into the reactor is 0.8Mpa. Under the action of gas with certain pressure, the adsorbent expands after being filled with the gas. In particular, the gas added in the reactor may be air, nitrogen or carbon dioxide. The liquid phase foaming agent is added into the adsorbent to be a hydrofluorocarbon, so that the acidity of the adsorbent can be regulated, the adsorbent can be expanded rapidly, and the aim of desorption is fulfilled.
And S4, introducing hot steam into the reactor. In order to make the adsorbent react quickly, the steam temperature of the adsorbent in the reactor is gradually increased to a preset temperature. Specifically, the preset temperature is 120 ℃. The adsorbent expands first and then the temperature of the adsorbent rises, so that the organic matters adsorbed in the adsorbent are quickly separated from the adsorbent under the internal and external acting forces of internal expansion and external temperature rise, and the desorption is complete.
And S5, continuously introducing waste heat steam while discharging the gas in the reactor so as to enable the waste heat steam to continuously act, enabling the low-pressure waste heat steam to serve as desorption external temperature, and carrying out desorption through high-temperature steam or adjusting the desorbed acidity. The preset time period of the continuously-introduced waste heat steam is 25-35min. Preferably, in this embodiment, the period of time for continuously introducing the waste heat steam is 30min.
And S6, after the desorption is finished, discharging condensed water generated in the reactor after the cooling of the hot steam.
Specifically, in this embodiment, the inorganic foaming agent is an inorganic foaming agent solution. The inorganic foaming agent solution can be attached to the adsorbent by spraying.
Specifically, in this embodiment, the adsorbent is activated carbon or an aluminum-silicon porous inorganic material. The active carbon is a black porous solid carbon, and is produced by crushing, molding or carbonizing and activating coal with uniform coal particles. The main component is carbon, and contains a small amount of elements such as oxygen, hydrogen, sulfur, nitrogen, chlorine and the like. Has strong adsorption performance and is an adsorbent with extremely wide application. The active carbon is a very fine carbon particle with a large surface area, and the carbon particle also has finer pores-capillaries. The capillary tube has strong adsorption capacity, and can be fully contacted with gas (impurities) due to the large surface area of the carbon particles. When these gases (impurities) hit the capillary tube, they are adsorbed, and act as a purification.
The aluminum-silicon porous inorganic material is an artificial inorganic nonmetallic material with tiny pores, light weight and large surface area, and has the characteristics of good adsorption and purification capability.
The desorption process after the adsorption saturation of the adsorbent provided by the embodiment of the invention ensures that the organic matters adsorbed in the adsorbent are rapidly transferred to an external gas phase or a liquid phase through the internal and external desorption forces of gas and steam, and the desorption efficiency is excellent by adopting the internal gas expansion and the external steam heating after the adsorbent reaches the adsorption capacity limit; compared with the traditional organic wastewater adsorption and desorption process, the method has remarkable advantages in engineering investment and running cost entropy, meanwhile, unattended operation can be achieved, and the degree of automation is extremely high.
The foregoing is merely illustrative of the present invention, and the present invention is not limited thereto, and any changes or substitutions easily contemplated by those skilled in the art within the scope of the present invention should be included in the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (6)
1. A desorption process after adsorption saturation of an adsorbent, comprising the steps of:
step S1, washing the adsorbent clean water after adsorption saturation in organic wastewater;
step S2, air purging the adsorbent surface liquid;
s3, placing the adsorbent into a reactor, introducing gas into the reactor to pressurize the adsorbent, and stopping;
step S4, hot steam is introduced into the reactor;
step S5, continuously introducing waste heat steam while discharging the gas in the reactor;
s6, discharging condensed water after desorption is finished;
in the step S3, the preset time period for pressurizing the adsorbent by introducing gas into the reactor is 10-20min, and the pressure of the introduced gas is 0.4-2.0MPa;
also includes a step S31 of adding an inorganic foaming agent or a liquid-phase foaming agent after the adsorbent is placed in the reactor.
2. The desorption process after the adsorption saturation of the adsorbent according to claim 1, further comprising step S21, wherein the adsorbent is cooled at normal temperature after the surface liquid of the adsorbent is purged with air.
3. The desorption process after the adsorption saturation of the adsorbent according to claim 1, wherein the inorganic foaming agent is an inorganic foaming agent solution.
4. The desorption process after the adsorption saturation of the adsorbent according to claim 1, wherein in step S3, the vapor temperature of the adsorbent in the reactor is gradually increased to a preset temperature.
5. The desorption process after the adsorption saturation of the adsorbent according to claim 1, wherein in the step S5, the time for continuously introducing the residual heat steam is 25 to 35 minutes.
6. The desorption process after the adsorption saturation of the adsorbent according to claim 1, wherein the adsorbent is activated carbon or an aluminum silicon porous inorganic material.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110616745.0A CN113304737B (en) | 2021-06-02 | 2021-06-02 | Desorption process after adsorption saturation of adsorbent |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110616745.0A CN113304737B (en) | 2021-06-02 | 2021-06-02 | Desorption process after adsorption saturation of adsorbent |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN113304737A CN113304737A (en) | 2021-08-27 |
| CN113304737B true CN113304737B (en) | 2023-05-23 |
Family
ID=77377079
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110616745.0A Active CN113304737B (en) | 2021-06-02 | 2021-06-02 | Desorption process after adsorption saturation of adsorbent |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113304737B (en) |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH1133335A (en) * | 1997-07-24 | 1999-02-09 | Mitsubishi Heavy Ind Ltd | Method and apparatus for treating gas with inorganic adsorbent |
| DE19834945A1 (en) * | 1998-08-03 | 2000-02-17 | Buck Werke Gmbh & Co I K | Continuous biological purification and re-use of waste water containing surfactant, e.g. from laundry, involves adsorbing impurities and regenerating adsorbent suspension in bioreactor |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN206688478U (en) * | 2017-05-18 | 2017-12-01 | 长春工程学院 | Synchronous photoelectromagnetic desulphurization denitration adsorption tower |
| CN108970596A (en) * | 2018-08-16 | 2018-12-11 | 无锡四方集团有限公司 | The desorption and regeneration technique in situ of the adsorbent of organic matter in adsorbed water body |
| CN109482036A (en) * | 2018-11-06 | 2019-03-19 | 无锡四方集团有限公司 | A kind of adsorption treatment of organic exhaust gas and its desorption and regeneration technique of adsorbent |
| CN109205728A (en) * | 2018-11-07 | 2019-01-15 | 无锡四方集团有限公司 | The technique and equipment of active carbon in-situ desorption and regeneration after a kind of activated carbon adsorption organic matter soluble in water and adsorption saturation |
| CN112090952B (en) * | 2020-08-29 | 2021-07-27 | 山西大学 | Boiling type micro-foam soil pollution desorption device and method suitable for coking field |
-
2021
- 2021-06-02 CN CN202110616745.0A patent/CN113304737B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH1133335A (en) * | 1997-07-24 | 1999-02-09 | Mitsubishi Heavy Ind Ltd | Method and apparatus for treating gas with inorganic adsorbent |
| DE19834945A1 (en) * | 1998-08-03 | 2000-02-17 | Buck Werke Gmbh & Co I K | Continuous biological purification and re-use of waste water containing surfactant, e.g. from laundry, involves adsorbing impurities and regenerating adsorbent suspension in bioreactor |
Also Published As
| Publication number | Publication date |
|---|---|
| CN113304737A (en) | 2021-08-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| TWI787509B (en) | A method for hydrogen extraction and reuse of LED-MOCVD process exhaust gas with full temperature range pressure swing adsorption | |
| CN103920365B (en) | Nitrogen in variable-frequency variable-voltage absorption recovery roasting pyrite furnace gas and the method for sulfur dioxide | |
| CN101700878B (en) | Nitrogen purification method | |
| KR20080061359A (en) | Process and apparatus for the purification of methane rich gas streams | |
| CN107866199B (en) | Carbon molecular sieve for adsorption and dehydration of liquefied gas and preparation method thereof | |
| CA2675833A1 (en) | Method and plant for treating crude gas, in particular biogas, containing methane and carbon dioxide, in order to produce methane | |
| WO2022160792A1 (en) | Cold rolling annealing furnace waste hydrogen recycling system and cold rolling annealing furnace hydrogen supply system | |
| CN106955595B (en) | Regeneration method of desulfurizer elemental sulfur in desulfurizing tower | |
| CN104918680A (en) | Method and device for removing absorbable gases from pressurized industrial gases contaminated with absorbable gases, wihout supplying cooling energy | |
| CN105056708A (en) | Novel temperature and pressure variable adsorption technology | |
| CN111909745A (en) | Molecular sieve dehydration device and dehydration process for dry gas internal circulation regeneration | |
| CN101439280B (en) | Expanded graphite-based composite material and preparation method thereof | |
| CN116059784A (en) | Method and system for capturing carbon dioxide in flue gas by pressure swing adsorption | |
| CN113304737B (en) | Desorption process after adsorption saturation of adsorbent | |
| JPWO2014181860A1 (en) | Method for separating methane and nitrogen | |
| CN110407207B (en) | High-temperature co-carbonizing agent and application thereof in recarburization and impurity solidification in carbonization process of plastic wastes | |
| CN101973603B (en) | Desorption method for reutilization of desorption agent | |
| CN111214926A (en) | Waste gas recovery processing system and method based on LNG cold energy utilization | |
| WO2013030946A1 (en) | Adsorbent and method for producing same | |
| KR101531605B1 (en) | A second-stage membrane process and an apparatus for the production of high purity methane gas using low operation pressure and temperature conditions | |
| CN114212961B (en) | Sludge micro-positive pressure carbonization control system and gas purification method | |
| Mutunga et al. | Technologies for Biogas Upgrading to Biomethane: A Review | |
| CN102728320A (en) | Preparation method for modified porous bamboo charcoal materials used for separating carbon dioxide and methane | |
| CN110102275A (en) | A kind of method of hydroxyl radical free radical regeneration gold mine waste active carbon | |
| CN210001582U (en) | Low-moisture-content hydrogen chloride synthesis system |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |