CN103664964B - The absorption process of triethylene diamine production rectifying gas and device - Google Patents
The absorption process of triethylene diamine production rectifying gas and device Download PDFInfo
- Publication number
- CN103664964B CN103664964B CN201310699672.1A CN201310699672A CN103664964B CN 103664964 B CN103664964 B CN 103664964B CN 201310699672 A CN201310699672 A CN 201310699672A CN 103664964 B CN103664964 B CN 103664964B
- Authority
- CN
- China
- Prior art keywords
- absorption
- gas
- lyosorption
- liquid
- triethylene diamine
- 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
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D487/00—Heterocyclic compounds containing nitrogen atoms as the only ring hetero atoms in the condensed system, not provided for by groups C07D451/00 - C07D477/00
- C07D487/02—Heterocyclic compounds containing nitrogen atoms as the only ring hetero atoms in the condensed system, not provided for by groups C07D451/00 - C07D477/00 in which the condensed system contains two hetero rings
- C07D487/08—Bridged systems
-
- 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
- B01D53/1406—Multiple stage absorption
-
- 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
- B01D53/1493—Selection of liquid materials for use as 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
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/205—Other organic compounds not covered by B01D2252/00 - B01D2252/20494
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/50—Combinations of absorbents
- B01D2252/504—Mixtures of two or more absorbents
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The present invention relates to absorption process and the device of triethylene diamine production rectifying.Involved method comprises: first order absorption, secondary absorb and three grades of absorptions; First order absorption utilizes the production rectifying gas of the first lyosorption to triethylene diamine to absorb; Secondary absorbs the second lyosorption to absorbing without the gas absorbed after first order absorption separation; Three grades absorb the 3rd lyosorption to absorbing without the gas absorbed after secondary absorption extraction.The absorption unit of involved triethylene diamine production rectifying comprises and is communicated with first order absorption equipment, secondary absorption equipment and three grades of absorption equipments successively.Wherein three grades of absorption equipments comprise vacuum pump and gas-liquid separation device, and gas-liquid separation device carries out gas-liquid separation to the liquid exported in vacuum pump, and isolated Liquid transfer enters secondary absorption equipment and is used as the second lyosorption.Absorption process of the present invention and device can make rectifying tower quiet run, economize on resources.
Description
Technical field
The invention belongs to chemical technology field, be specifically related to a kind of absorption unit and method of triethylene diamine production rectifying.
Background technology
Triethylene diamine (TEDA) is the whipping agent producing flexible polyurethane, semihard, rigid foam, is also used to ethylene rolymerization catalyst, coating and plastics etc.
The chemical structural formula of triethylene diamine:
At present, the raw materials of triethylene diamine is mainly N-hydroxyethyl piperazine, quadrol, thanomin, piperazine etc.Triethylene diamine fusing point is 158 DEG C, and boiling point 174 DEG C, has the tendency that strongly distils.When usual triethylene diamine adopts conventional vacuum rectifying separation, this easy crystallization, easily solidify, the component that easily distils often blocks vacuum pipeline or material conveying pipe, cause Rectification column pressure to be difficult to control, distillation procedure can not stably be carried out.Require these blocking materials of removing, must run by arrestment, therefore can reduce the production efficiency of equipment.
In prior art, corresponding separation scheme can be taked according to the different methods preparing triethylene diamine.ZL200580015592.3, CN200680045704.4, ZL02817896.3, ZL02117652.3 report the preparation method of high-purity triethylene diamine respectively.Its basic skills is first gasified in rectifying tower by the product stream containing TEDA, introduces in liquid solvent, normally pentane or hexanaphthene by the TEDA of gaseous state by down-film condenser equipment, and crystallization TEDA from the liquor produced, provides highly purified TEDA subsequently.Concrete absorption technique method is not all related in prior art.
Contriver finds, when adopting vacuum pump to reduce pressure to triethylene diamine rectifying tower, the vacuum pipeline that the volatile components such as triethylene diamine wherein, liquid solvent can stretch out from rectifying tower top enters vacuum system; When using water as pendular ring medium, the organic constituent in tail gas enters in pendular ring medium, when directly discharging, not only causing serious environmental pollution around, and wasting resource.
Summary of the invention
For defect or the deficiency of prior art, an object of the present invention is the absorption unit providing a kind of triethylene diamine production rectifying.
For this reason, the absorption process of triethylene diamine production rectifying gas provided by the invention comprises:
First order absorption, utilizes the production rectifying gas of the first lyosorption to triethylene diamine to absorb;
Secondary absorbs, and utilizes the second lyosorption to absorbing without the gas absorbed after first order absorption separation;
Three grades of absorptions, utilize the 3rd lyosorption to absorbing without the gas absorbed after secondary absorption extraction.
Described three grades of absorption liquids absorbed are used as the second lyosorption after gas-liquid separation.
Described three grades of absorptions comprise utilize after secondary absorption extraction without the gas absorbed as the compression ring medium of vacuum pump, utilize the pendular ring medium of vacuum pump to absorb the unabsorbed gases after secondary absorption extraction as the 3rd lyosorption, absorption liquid is used as the second lyosorption after gas-liquid separation simultaneously.
Described first lyosorption is one or more the combination in hexanaphthene, toluene, dimethylbenzene, sym-trimethylbenzene, naphthane and sherwood oil.
The pendular ring medium of described vacuum pump is amino alcohol compound, as thanomin, hydroxyethylethylene diamine, diethanolamine or trolamine.
The temperature of described first order absorption is 60 DEG C ~ 80 DEG C; The operating pressure of described vacuum pump is 30kPa ~ 50kPa.
For defect or the deficiency of prior art, another object of the present invention is to the absorption unit that a kind of triethylene diamine production rectifying is provided.
For this reason, the absorption unit of triethylene diamine production rectifying provided by the invention comprises and is communicated with first order absorption equipment, secondary absorption equipment and three grades of absorption equipments successively.
Described first order absorption equipment comprises falling-film absorber; Be provided with many root absorption pipe in described falling-film absorber, the top ingress of every root absorption pipe is provided with film applicator; Described film applicator comprises pipe, and the outer wall of this pipe offers spiral grooves, and liquid enters absorption tube along this spiral grooves.
Described secondary absorption equipment comprises packed absorber, the gas in this packed absorber and liquid backmixing; Described packing material absorbing tower bottom is provided with phase separator; Temperature in described phase separator is 25 DEG C ~ 30 DEG C.
Described three grades of absorption equipments comprise vacuum pump and gas-liquid separation device, and described gas-liquid separation device carries out gas-liquid separation to the liquid exported in vacuum pump, and isolated Liquid transfer enters secondary absorption equipment and is used as the second lyosorption.
Compared with prior art, beneficial effect of the present invention is:
(1) absorption of triethylene diamine production rectifying provided by the invention and the processing method that vacuumizes, carry out at the spray-absorption of triethylene diamine production rectifying, enable rectifying tower quiet run in three grades of absorption equipments;
(2) the present invention uses amino alcohol compound as the triethylene diamine in absorption agent recovery tail gas and volatile components, utilize the density difference of the second absorption agent and the first absorption agent and realize being separated, and the second absorption agent and the first absorption agent are all recycled, be conducive to reducing discharge of wastewater and environmental pollution, economize on resources, reduce Material Cost.
(3) the present invention utilizes the 3rd lyosorption to absorbing without the gas absorbed after secondary absorption extraction, the pendular ring medium added is as the 3rd lyosorption, be conducive to the absorption completely realizing coagulating component, absorption liquid is used as the second lyosorption through gas-liquid separation Posterior circle, and material is fully recycled.
To sum up, absorption process of the present invention or device can make rectifying tower quiet run, and use amino alcohol to reclaim triethylene diamine, the liquid solvent in tail gas as absorption agent, are conducive to reducing environmental pollution, economize on resources.
Accompanying drawing explanation
Below in conjunction with accompanying drawing and embodiment, explanation is further explained to the present invention.
Fig. 1 is the spray-absorption device structural reference schematic diagram of triethylene diamine production rectifying of the present invention;
Each coded representation in figure: 1-falling-film absorber; 2-packed absorber; 3-phase separator; 4-vacuum pump; 5-gas-liquid separator; A, b, c, d, e, f, g, h, i, j, k are pipeline.
Fig. 2 is film applicator structural representation of the present invention.
Embodiment
The production rectifying gas of triethylene diamine of the present invention is the gaseous phase materials of triethylene diamine rectifying tower extraction, generally comprise triethylene diamine, a small amount of light constituent piperazine, methylpiperazine, ethyl piperazidine, heavy constituent N-aminoethyl piperazine, and other non-condensable gases.
Separate absorbent device of the present invention is generally the operating unit in triethylene diamine separation and purification, and is connected with reaction unit.As required, one or more pre-separation unit can be added between reaction unit and triethylene diamine rectification cell.Separate absorbent device is connected by pipeline with the partial condenser of triethylene diamine rectifying tower, and partial condenser to be positioned at above rectifying tower top and to be directly connected with rectifying tower.
As shown in Figure 1, the spray-absorption of triethylene diamine production rectifying of the present invention carries out in three grades of absorption equipments, wherein first step absorption equipment is falling-film absorber 1, second stage absorption equipment is the packed absorber 2 of bottom with phase separator 3, third stage absorption equipment comprises vacuum pump 4 and gas-liquid separator 5, carry out in the device that vacuum pumping method is made up of vacuum pump and gas-liquid separator, gas-liquid separator carries out gas-liquid separation to the liquid exported in vacuum pump, isolated liquid is discharged from gas-liquid separator, be conveyed into secondary absorption equipment and be used as the second lyosorption, the second absorption agent after absorbing gas flows in the phase separator 3 of bottom, and divides mutually in phase separator 3, fresh pendular ring medium in vacuum system is used for the 3rd absorption agent of second stage absorption equipment.
First lyosorption of the present invention is non-polar hydrocarbon kind solvent, one or more in preferred hexanaphthene, toluene, dimethylbenzene, sym-trimethylbenzene, naphthane, sherwood oil.
Second lyosorption of the present invention is amino alcohol, identical with vacuum pump pendular ring medium, preferred alcohol amine, hydroxyethylethylene diamine, diethanolamine or trolamine.
First order absorption equipment of the present invention comprises falling-film absorber 1; Many root absorption pipe is installed in falling-film absorber 1, absorption tube has extension higher than falling-film absorber tube sheet place, trilateral overflow weir is had around the tube wall of absorption tube extension, its quantity is evenly arranged around pipe, overflow weir perforate number is generally 3 ~ 4, and the top ingress of every root absorption pipe is provided with film applicator.
As shown in Figure 2, film applicator structure of the present invention is pipe 6, and pipe 6 top connects overcoat annulus, and by arch brace in absorption tube top, pipe 6 is carved with spiral grooves, preferably equidistant spiral grooves.The width of usual spiral grooves, the degree of depth and number are by the unit time, and the liquid bulk accumulated amount of unit perimeter circulation determines, preferably, the spiral grooves width of film applicator of the present invention is 3 ~ 5mm, and the degree of depth is 4 ~ 6mm, and spiral grooves number is 3 ~ 4.The gap formed between film applicator and absorption tube inwall makes liquid film forming, when liquid flows through spiral type groove, forms spiral motion, is conducive to liquid homogeneous film formation in absorption tube.
The preferred device working process of the present invention is that the process gas from triethylene diamine rectifying tower top enters film applicator center cavity, then enters absorption tube tube side; First lyosorption is entered when absorption tube tube side flows through spiral type groove by liquid flow hole and forms spiral motion, and make it in absorption tube inwall film forming, process gas and the first lyosorption are at falling-film absorber tube side and flow absorption, and the liquor formed after absorbing is decrystallized system;
The mixed gas that in first absorption equipment, unabsorbed process gas and the first lyosorption volatiles form, enter packed absorber bottom, contact with from second absorption agent on packed absorber top is reverse, the second absorption agent after absorbing above-mentioned gas flows in the phase separator of bottom, and divide mutually in phase separator, upper strata is the organic phase being rich in the first absorption agent, and lower floor is that the organic phase being rich in the second absorption agent discharges system process respectively;
In second absorption equipment, unabsorbed noncondensable gas is discharged by packing material absorbing column overhead, enter the vacuum pump of third stage absorption equipment, the fresh pendular ring medium added with enter gas-liquid separator in the lump after, not solidifying part is discharged through gas-liquid separator top, pendular ring medium after separation is discharged by bottom gas-liquid separator, be circulated to the second absorption equipment, wherein the second absorption agent of packing material absorbing tower top is from the pendular ring medium of the discharge of vacuum system.
In third stage absorption equipment, utilize the 3rd lyosorption to absorbing without the gas absorbed after secondary absorption extraction, the fresh pendular ring medium added is as the 3rd lyosorption.
Below the embodiment that contriver provides, to be further explained explanation to technical scheme of the present invention.
embodiment 1:
The spray-absorption of triethylene diamine production rectifying carries out in two-stage absorption equipment, and wherein first step absorption equipment is falling-film absorber 1, and its top is pipe shell side structure, and bottom is cavity structure,
Second stage absorption equipment is the packed absorber 2 of bottom with phase separator 3, and phase separator 3 inside is with separation dividing plate, and after mutually light and heavy phase realization is separated, dividing plate realizes light phase overflow in phase separator; Packed absorber is built with regular or random packing (as Stainless Steel Cloth or Mellapak packing or θ ring), and wire feeding can be selected as required.
Carry out in the vacuum system that vacuum pumping method is made up of liquid-ring vacuum pump 4 and gas-liquid separator 5, vacuum pump regulates pressure to be 30kPa ~ 50kPa, and the pendular ring medium in vacuum system is used for the absorption agent of second stage absorption equipment;
Process gas from triethylene diamine rectifying tower top enters falling-film absorber 1 top by pipeline a, absorption is flowed at falling-film absorber 1 tube side with the first lyosorption from line b, general control temperature is 20 DEG C ~ 100 DEG C, preferably 60 DEG C ~ 80 DEG C, the liquor formed after absorbing is discharged by bottom falling-film absorber, to decrystallize system through line c;
The mixed gas that in first absorption equipment, unabsorbed process gas and the first lyosorption volatiles form, enters packed absorber 2 bottom by pipeline d; The second absorption agent from pipeline j enters packed absorber 2 and pushes up, the two is full regression contact in packed absorber, the second absorption agent after absorbing above-mentioned gas flows in the phase separator 3 of bottom, and divide mutually in phase separator, control temperature in phase separator is 20 DEG C ~ 40 DEG C, preferably 25 DEG C ~ 30 DEG C, upper strata is the organic phase being rich in the first absorption agent, lower floor is the organic phase being rich in the second absorption agent, Posterior circle is discharged through pipeline f in upper strata after dividing plate liquid stream, lower floor, by after discharge bottom phase separator, is circulated to distillation system or reactive system through pipeline e.
In second absorption equipment, unabsorbed noncondensable gas is discharged by packing material absorbing column overhead, vacuum pump 4 is entered through pipeline g, vacuum pump regulates pressure to be 30kPa ~ 50kPa, fresh pendular ring medium required for vacuum pump is added by pipeline h, not solidifying component and pendular ring medium enter gas-liquid separator 5 by pipeline i, wherein not solidifying component is separated in gas-liquid separator 5 with pendular ring medium, not solidifying component is discharged through pipeline k, pendular ring medium is discharged by pipeline j after gas-liquid separator separates, is cycled to used in the second absorption agent of packing material absorbing tower top.
In third stage absorption equipment, utilize the 3rd lyosorption to absorbing without the gas absorbed after secondary absorption extraction, the fresh pendular ring medium added is as the 3rd lyosorption.
embodiment 2:
From the process gas of triethylene diamine rectifying tower top, percent mass forms: TEDA is 97.2%, PIP is 0.7%, other component is 2.0%, enter falling-film absorber top from pipeline a with 92.6kg/h, flows absorption with the toluene from line b with 303.1kg/h at falling-film absorber tube side, the temperature controlling falling-film absorber is 68 DEG C, formed containing the toluene solution of TEDA after absorbing, TEDA percentage composition is 23.8%, to decrystallize system from line c with 358.6kg/h.
The mixed gas that in first absorption equipment, unabsorbed process gas and the first lyosorption volatiles form, enter packed absorber with 37.1kg/h, its percent mass forms: PIP is 1.97%, TEDA is 12.2%, other component is 5.01%, and all the other are toluene gas; Thanomin from pipeline j enters packing material absorbing tower top with 259.3kg/h, the two is full regression contact in packed absorber, the second absorption agent after absorbing above-mentioned gas flows in the phase separator 3 of bottom, and divide mutually dividing in device mutually, divide the temperature of device to be 26 DEG C mutually, upper strata is rich in toluene component and is discharged from pipeline f with 29.8kg/h, thanomin component phase percent mass composition is rich in lower floor: PIP is 0.25%, TEDA is 1.71%, and all the other are thanomin, discharges from pipeline e with 264.5kg/h;
In second absorption equipment, unabsorbed noncondensable gas is discharged by packing material absorbing column overhead, vacuum pump is entered with 1.9kg/h, vacuum pump regulates pressure to be 50kPa, thanomin is added with 260.0kg/h by pipeline h, not solidifying component and thanomin enter gas-liquid separator 5 by pipeline i, and not solidifying component is separated in gas-liquid separator 5 with pendular ring medium, and not solidifying component is discharged through pipeline k, pendular ring medium is discharged by pipeline j after gas-liquid separator separates, is cycled to used in the second absorption agent of packing material absorbing tower top.
In third stage absorption equipment, utilize the 3rd lyosorption to absorbing without the gas absorbed after secondary absorption extraction, the fresh pendular ring medium added is as the 3rd lyosorption.
embodiment 3:
From the process gas of triethylene diamine rectifying tower top, percent mass forms: TEDA is 97.2%, PIP is 0.7%, other component is 2.0%, enter falling-film absorber top from pipeline a with 92.6kg/h, flows absorption with the sym-trimethylbenzene from line b with 253.1kg/h at falling-film absorber tube side, the temperature controlling falling-film absorber is 76 DEG C, formed containing the sym-trimethylbenzene solution of TEDA after absorbing, TEDA percentage composition is 27.6%, to decrystallize system from line c with 309.8kg/h.
The mixed gas that in first absorption equipment, unabsorbed process gas and the first lyosorption volatiles form, enter packed absorber with 35.9kg/h, its percent mass forms: PIP is 1.81%, TEDA is 12.5%, other component is 5.15%, and all the other are sym-trimethylbenzene gas; Hydroxyethylethylene diamine from pipeline j enters packing material absorbing tower top with 251.2kg/h, the two is full regression contact in packed absorber, the second absorption agent after absorbing above-mentioned gas flows in the phase separator 3 of bottom, and divide mutually dividing in device mutually, the temperature of device is divided to be 22 DEG C mutually, upper strata is rich in sym-trimethylbenzene component and is discharged from pipeline f with 28.8kg/h, hydroxyethylethylene diamine component phase percent mass composition is rich in lower floor: PIP is 0.26%, TEDA is 1.75%, all the other are hydroxyethylethylene diamine, discharge from pipeline e with 256.4kg/h;
In second absorption equipment, unabsorbed noncondensable gas is discharged by packing material absorbing column overhead, vacuum pump is entered with 1.9kg/h, vacuum pump regulates pressure to be 50kPa, hydroxyethylethylene diamine is added with 260.0kg/h by pipeline h, not solidifying component and hydroxyethylethylene diamine enter gas-liquid separator 5 by pipeline i, not solidifying component is separated in gas-liquid separator 5 with hydroxyethylethylene diamine, not solidifying component is discharged through pipeline k, hydroxyethylethylene diamine is discharged by pipeline j after gas-liquid separator separates, is cycled to used in the second absorption agent of packing material absorbing tower top.
In third stage absorption equipment, utilize the 3rd lyosorption to absorbing without the gas absorbed after secondary absorption extraction, the fresh pendular ring medium added is as the 3rd lyosorption.
Claims (3)
1. an absorption process for triethylene diamine production rectifying gas, it is characterized in that, method comprises:
First order absorption, utilizes the production rectifying gas of the first lyosorption to triethylene diamine to absorb;
Secondary absorbs, and utilizes the second lyosorption to absorbing without the gas absorbed after first order absorption separation;
Three grades of absorptions, utilize the 3rd lyosorption to absorbing without the gas absorbed after secondary absorption extraction;
Reclaim first order absorption liquid and secondary absorption liquid;
Described three grades of absorptions comprise utilize after secondary absorption extraction without the gas absorbed as the compression ring medium of vacuum pump, utilize the pendular ring medium of vacuum pump to absorb the unabsorbed gases after secondary absorption extraction as the 3rd lyosorption, absorption liquid is used as the second lyosorption after gas-liquid separation simultaneously;
Described first lyosorption is one or more the combination in hexanaphthene, toluene, dimethylbenzene, sym-trimethylbenzene, naphthane and sherwood oil;
The pendular ring medium of described vacuum pump is amino alcohol compound, and described amino alcohol compound is selected from thanomin, hydroxyethylethylene diamine, diethanolamine or trolamine.
2. the absorption process of triethylene diamine production rectifying gas as claimed in claim 1, it is characterized in that, the temperature of described first order absorption is 60 DEG C ~ 80 DEG C; The operating pressure of described vacuum pump is 30kPa ~ 50kPa.
3. an absorption unit for triethylene diamine production rectifying gas, is characterized in that, device comprises and is communicated with first order absorption equipment, secondary absorption equipment and three grades of absorption equipments successively;
Described first order absorption equipment comprises falling-film absorber; Be provided with many root absorption pipe in described falling-film absorber, the top ingress of every root absorption pipe is provided with film applicator; Described film applicator comprises pipe, and the outer wall of this pipe offers spiral grooves, and liquid enters absorption tube along this spiral grooves;
Described secondary absorption equipment comprises packed absorber, the gas in this packed absorber and liquid backmixing; Described packing material absorbing tower bottom is provided with phase separator; Temperature in described phase separator is 25 DEG C ~ 30 DEG C;
Described three grades of absorption equipments comprise vacuum pump and gas-liquid separation device, and described gas-liquid separation device carries out gas-liquid separation to the liquid exported in vacuum pump, and isolated Liquid transfer enters secondary absorption equipment and is used as the second lyosorption.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310699672.1A CN103664964B (en) | 2013-12-18 | 2013-12-18 | The absorption process of triethylene diamine production rectifying gas and device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310699672.1A CN103664964B (en) | 2013-12-18 | 2013-12-18 | The absorption process of triethylene diamine production rectifying gas and device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103664964A CN103664964A (en) | 2014-03-26 |
| CN103664964B true CN103664964B (en) | 2016-03-02 |
Family
ID=50303830
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310699672.1A Active CN103664964B (en) | 2013-12-18 | 2013-12-18 | The absorption process of triethylene diamine production rectifying gas and device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103664964B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112387077B (en) * | 2020-11-13 | 2022-07-15 | 西安近代化学研究所 | Tail gas absorption device and method for distillation tower for producing ethyleneimine |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3128275A (en) * | 1962-06-07 | 1964-04-07 | Jefferson Chem Co Inc | Method for the purification of triethylenediamine |
| US3993651A (en) * | 1975-03-17 | 1976-11-23 | Texaco Development Corporation | Triethylenediamine recovery |
| DE10100943A1 (en) * | 2001-01-10 | 2002-07-11 | Basf Ag | Production of a solution of pure triethylenediamine comprises evaporation from a mixture comprising a solvent or a diluent having a specified boiling point at normal pressure |
| DE10122502A1 (en) * | 2001-05-10 | 2002-11-14 | Basf Ag | Purification of triethylene diamine, useful as a catalyst for the production of polyurethane foam, comprises crystallization and extraction of the resulting mother liquor with an extraction agent |
| DE102004024274A1 (en) * | 2004-05-15 | 2005-12-01 | Basf Ag | Process for the preparation of a solution of pure triethylenediamine (TEDA) |
| DE102005061956A1 (en) * | 2005-12-23 | 2007-07-05 | Basf Ag | Processing of triethylene diamine, useful as catalyst to prepare polyurethane foams, comprises introducing the gaseous triethyl diamine into a solvent, crystallizing and separating the mixture and extracting the obtained mother liquor |
| CN102584834A (en) * | 2011-12-20 | 2012-07-18 | 西安近代化学研究所 | Separation method for mixture of triethylene-diamine and ethanolamine |
| CN103012412B (en) * | 2012-11-21 | 2014-08-27 | 西安近代化学研究所 | Separation method of triethylene diamine and ethanolamine azeotrope |
| CN102977108B (en) * | 2012-11-21 | 2014-12-10 | 西安近代化学研究所 | Method for separating triethylene diamine and ethanolamine |
-
2013
- 2013-12-18 CN CN201310699672.1A patent/CN103664964B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN103664964A (en) | 2014-03-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103724155B (en) | A kind of production technique of propenyl chloride | |
| CN102101651B (en) | Method and device for refining chlorine hydride byproduct and recovering trifluoromethane in production of monochlorodifluoromethane | |
| CN204746030U (en) | Carbon dioxide gas's device is absorbed to sled dress formula suitable for platform | |
| CN111333530B (en) | Heat pump rectification process for recycling DMAC (dimethylacetamide) or DMF (dimethyl formamide) waste liquid | |
| CN105906512B (en) | A kind of the single column separating technology and device of phenylenediamine isomer | |
| CN108586190A (en) | A method of recycling chloromethanes from chloromethanes exhaust gas | |
| CN103333056B (en) | Method and device for deeply removing sulfide in MTBE | |
| CN108654130A (en) | The method and apparatus of NMP recycling heat pump distillation in a kind of production of lithium electricity | |
| CN111100004B (en) | Method and integrated device for refining dimethyl carbonate | |
| CN103664964B (en) | The absorption process of triethylene diamine production rectifying gas and device | |
| CN105152860A (en) | Method for refining mixed alcohol by rectification-pervaporation coupling process | |
| CN105647583A (en) | Novel absorption stabilizing technology and system | |
| CN100491245C (en) | Method for preparing liquid carbon dioxide in foodstuff level by using tail gas of cement kiln | |
| CN102126958B (en) | Device and method for preparing high purity m/p-nitrotoluene by coupling rectification and crystallization | |
| CN104923026B (en) | Polysilicon tail gas recovering method and device thereof | |
| CN111892525A (en) | N-methyl pyrrolidone for liquid crystal panel and production process thereof | |
| CN114432728B (en) | System and process for purifying NMP | |
| CN102924225B (en) | Method for selectively absorbing and separating mixed toluene dichloride | |
| CN206940774U (en) | A kind of tetrahydrofuran dehydration device | |
| CN103877829B (en) | The absorption process of ethylenediamine rectifying column tail gas and device | |
| CN203959827U (en) | Tripping device for process for preparation of CS 2 molten sulfur | |
| CN102701920A (en) | Method for purifying vinyl isobutyl ether | |
| CN109134405B (en) | Waste heat recovery equipment and process utilizing MVR technology | |
| CN105712820A (en) | Novel technology for concentrating post-MTBE C4 | |
| CN111013309B (en) | Method for purifying tail gas and recovering materials in pivaloyl chloride production process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |