CN110787836A - Method for prolonging service cycle of catalyst for heptafluoropropane synthesis - Google Patents
Method for prolonging service cycle of catalyst for heptafluoropropane synthesis Download PDFInfo
- Publication number
- CN110787836A CN110787836A CN201911118665.1A CN201911118665A CN110787836A CN 110787836 A CN110787836 A CN 110787836A CN 201911118665 A CN201911118665 A CN 201911118665A CN 110787836 A CN110787836 A CN 110787836A
- Authority
- CN
- China
- Prior art keywords
- catalyst
- heptafluoropropane
- ahf
- reactor
- controlled
- 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
- 239000003054 catalyst Substances 0.000 title claims abstract 39
- UKACHOXRXFQJFN-UHFFFAOYSA-N heptafluoropropane Chemical compound FC(F)C(F)(F)C(F)(F)F UKACHOXRXFQJFN-UHFFFAOYSA-N 0.000 title claims abstract 22
- 238000000034 method Methods 0.000 title claims abstract 8
- 230000015572 biosynthetic process Effects 0.000 title claims 2
- 238000003786 synthesis reaction Methods 0.000 title claims 2
- 230000002194 synthesizing effect Effects 0.000 claims abstract 9
- 150000001412 amines Chemical class 0.000 claims abstract 4
- ZMANZCXQSJIPKH-UHFFFAOYSA-N Triethylamine Chemical compound CCN(CC)CC ZMANZCXQSJIPKH-UHFFFAOYSA-N 0.000 claims 12
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 claims 9
- 238000006243 chemical reaction Methods 0.000 claims 8
- 238000004821 distillation Methods 0.000 claims 4
- HCDGVLDPFQMKDK-UHFFFAOYSA-N hexafluoropropylene Chemical group FC(F)=C(F)C(F)(F)F HCDGVLDPFQMKDK-UHFFFAOYSA-N 0.000 claims 3
- 238000003756 stirring Methods 0.000 claims 2
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 claims 1
- 239000007789 gas Substances 0.000 claims 1
- 229910000040 hydrogen fluoride Inorganic materials 0.000 claims 1
- 239000000463 material Substances 0.000 claims 1
- ZMJUWFXCWLDAKQ-WZJLIZBTSA-N methyl 4-[[(3r,4s,5s,6r)-4,5-dihydroxy-7-[[4-(hydroxymethyl)phenyl]methyl]-1,1-dioxo-3,6-bis(phenoxymethyl)-1,2,7-thiadiazepan-2-yl]methyl]benzoate Chemical compound C1=CC(C(=O)OC)=CC=C1CN1S(=O)(=O)N(CC=2C=CC(CO)=CC=2)[C@H](COC=2C=CC=CC=2)[C@H](O)[C@@H](O)[C@H]1COC1=CC=CC=C1 ZMJUWFXCWLDAKQ-WZJLIZBTSA-N 0.000 claims 1
- 238000002156 mixing Methods 0.000 claims 1
- 238000000746 purification Methods 0.000 claims 1
- 150000003839 salts Chemical class 0.000 claims 1
- 238000000926 separation method Methods 0.000 claims 1
- 239000002904 solvent Substances 0.000 claims 1
- NTJBWZHVSJNKAD-UHFFFAOYSA-N triethylazanium;fluoride Chemical compound [F-].CC[NH+](CC)CC NTJBWZHVSJNKAD-UHFFFAOYSA-N 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims 1
- 239000007795 chemical reaction product Substances 0.000 abstract 1
- 239000000178 monomer Substances 0.000 abstract 1
- 230000002035 prolonged effect Effects 0.000 abstract 1
- 230000001502 supplementing effect Effects 0.000 abstract 1
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
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/20—Catalysts, in general, characterised by their form or physical properties characterised by their non-solid state
- B01J35/27—Catalysts, in general, characterised by their form or physical properties characterised by their non-solid state in a liquid or molten state
-
- 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
- B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
- B01J31/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
- B01J31/0234—Nitrogen-, phosphorus-, arsenic- or antimony-containing compounds
- B01J31/0235—Nitrogen containing compounds
- B01J31/0237—Amines
-
- 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
- B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
- B01J31/40—Regeneration or reactivation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/07—Preparation of halogenated hydrocarbons by addition of hydrogen halides
- C07C17/087—Preparation of halogenated hydrocarbons by addition of hydrogen halides to unsaturated halogenated hydrocarbons
-
- 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
- B01J2231/00—Catalytic reactions performed with catalysts classified in B01J31/00
- B01J2231/30—Addition reactions at carbon centres, i.e. to either C-C or C-X multiple bonds
- B01J2231/32—Addition reactions to C=C or C-C triple bonds
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a method for prolonging the service cycle of a catalyst for synthesizing heptafluoropropane, which comprises the following steps: (1) synthesizing a catalyst to form an AHF-amine catalyst system; (2) synthesizing heptafluoropropane in a catalyst of an AHF-amine catalyst system; (3) supplementing AHF, and recovering the molar ratio of AHF to amine in the catalyst; (4) separating the catalyst from the reaction product; (5) recovering the catalyst; according to the invention, AHF is supplemented before the catalyst and heptafluoropropane (F227) are separated, so that the standard molar ratio of a catalyst reactor is recovered, the amine monomer can be effectively prevented from being decomposed by the catalyst, the molar ratio of AHF to amine in an AHF-amine catalyst system is not disordered, the catalyst is not invalid, and the service cycle of the catalyst can be effectively prolonged.
Description
Technical Field
The present invention relates to a method for prolonging the service life of a catalyst for synthesizing heptafluoropropane (F227), which is used for prolonging the service life of the catalyst for synthesizing heptafluoropropane (F227).
Background
Heptafluoropropane is a clean gas chemical fire extinguishing agent which mainly uses chemical fire extinguishing and has physical fire extinguishing function, is colorless, tasteless, low-toxicity, non-conductive, free from polluting protected objects, free from damaging properties and precision facilities, and capable of reliably extinguishing B, C-type fires and electrical fires with low fire extinguishing concentration; the heptafluoropropane has small storage space, high critical temperature and low critical pressure, and can be liquefied and stored at normal temperature; the heptafluoropropane does not contain particles or oily residues after being released, has no destructive effect on the atmospheric ozone layer (ODP value is zero), and stays in the atmospheric layer for 31-42 years, thereby meeting the requirement of environmental protection.
The 1, 1, 1, 2, 3, 3, 3 heptafluoropropane is prepared by adding hexafluoropropylene under an AHF-amine composite system, the reaction can be carried out at normal temperature and normal pressure, the conversion rate, the selectivity and the yield can reach more than 99 percent, and the reaction is a typical green chemical reaction. The AHF-amine complex system is a catalyst system for preparing F227 (heptafluoropropane), and active ingredients of the catalyst system are gradually lost in the process of repeated use, so that the activity of the catalyst is gradually weakened, and finally the catalyst is ineffective. At present, a distillation tower is used for separating the catalyst from a reaction product in production, the catalyst is recovered, and the operation temperature of the distillation tower is strictly controlled so as to reduce the entrainment of effective components in the catalyst to a downstream working section.
In the production process of F227 (heptafluoropropane), the catalyst needs to be recycled, and the catalyst recycling process comprises the separation of the catalyst and a reaction product and the recycling of the catalyst. In the separation process of the catalyst and the reaction products, due to certain characteristics and equipment limitations of the catalyst, part of effective components in the catalyst can be entrained to a downstream working section in the separation process, so that the effective components in the catalyst are gradually lost, and the service life of the catalyst is influenced. The invention mainly utilizes an effective technical means to reduce the loss of effective components in the F227 catalyst, thereby prolonging the service life of the F227 catalyst. The prior art has the following disadvantages: the function of the evaporation tower is to separate the catalyst and the reaction product, leave most of the catalyst in the tower kettle and recycle the catalyst to the catalyst reaction kettle, and discharge more than 95% of F227 from the tower top to a downstream purification section. In the mixed material entering the distillation tower, as a part of AHF in the catalyst is reacted, the proportion of AHF in an AHF-amine catalyst system is reduced, the capability of combining AHF with amine is reduced, part of amine in the system can be decomposed into monomers, the amine monomers decomposed in the crude distillation process can be discharged into a downstream working section from the top of the tower, and the amine in the catalyst recycled to a catalyst reaction kettle can be reduced. The amines continue to decrease during catalyst recycle until the molar ratio of AHF to amine in the AHF-amine catalyst system is out of order, eventually leading to catalyst failure.
Disclosure of Invention
The technical problem to be solved by the invention is to provide a method for prolonging the service life of a catalyst for synthesizing heptafluoropropane (F227), wherein the service life of the catalyst is prolonged by reducing the loss of amine monomers in the catalyst.
In order to solve the above-mentioned technical problems, the method for extending the service life of a catalyst for the synthesis of heptafluoropropane (F227) according to the present invention comprises the steps of:
(1) preparing the catalyst in a catalyst reaction kettle to form an AHF-amine catalyst system. The catalyst system consists of AHF (anhydrous hydrogen fluoride), triethylamine and n-butanol, wherein salt generated by the reaction of the AHF and the triethylamine is the main component of the catalyst, and the n-butanol is the solvent of the catalyst. The molar ratio of AHF to triethylamine is controlled to be 2.5:1, and the mass ratio of triethylamine hydrogen fluoride to n-butanol is controlled to be 2.1: 1. The feeding sequence is that firstly, n-butyl alcohol is fed into a catalyst reaction kettle at one time, then triethylamine is fed into a catalyst reaction kettle at one time, after stirring and mixing are carried out uniformly, AHF is fed into the catalyst reaction kettle at the flow rate of 60-70 kg/h, the temperature of the catalyst reaction kettle is controlled to be 50-60 ℃, the pressure is controlled to be 0.05-0.1 MPa, and after the feeding is finished, stirring is carried out for 30min, and then the reaction is completed.
(2) Feeding the prepared catalyst into a heptafluoropropane reactor at one time, feeding hexafluoropropylene into the heptafluoropropane reactor at a flow rate of 400-500 kg/h, controlling the temperature of the reactor to be 50-65 ℃, controlling the pressure to be 0.15-0.3 MPa, and synthesizing the heptafluoropropane by using the hexafluoropropylene and AHF in the catalyst in a molar ratio of 1: 1.
Since the reaction process of AHF and catalyst is exothermic, in order to ensure the temperature in the F227 reactor to be controllable, the normal temperature circulating water cooling of the F227 reactor needs to be changed into the cooling of refrigerant below 5 ℃.
(3) After completion of the heptafluoropropane synthesis, a portion of the AHF in the catalyst has been consumed, for example: the addition of 1050kg of hexafluoropropene would require the consumption of 140kg of hydrogen fluoride, and in this case 140kg of additional hydrogen fluoride would be required in the heptafluoropropane reactor to restore the molar ratio of AHF to amine in the catalyst. When the AHF is supplemented, feeding the AHF into a heptafluoropropane reactor at a flow rate of 60-70 kg/h, controlling the temperature of the reactor to be 50-65 ℃ and controlling the pressure to be 0.15-0.3 MPa.
(4) And after the AHF feeding is finished and the reaction is completed, feeding the mixed material of the catalyst and the heptafluoropropane into a distillation tower for separation. The boiling point of the catalyst is more than 70 ℃, the boiling point of the heptafluoropropane is-16.4 ℃, and the catalyst and the heptafluoropropane can be separated in a distillation tower through the difference of the boiling points. The temperature of the distillation tower kettle is controlled to be 60-65 ℃, the top temperature is controlled to be 10-20 ℃, the pressure is controlled to be 0.05-0.15 MPa, and the catalyst and the heptafluoropropane can be separated.
(5) And (4) recovering the catalyst. And (3) when the pressure in the distillation tower is reduced to below 0.05MPa, the crude gas F227 in the tower top enters a downstream working section for purification, the catalyst in the tower kettle is cooled to 45-50 ℃ by circulating water and then is conveyed into an F227 reactor by a centrifugal pump for the next F227 synthesis.
The current process flow of F227 is catalyst synthesis, synthesis of F227 in a catalyst, separation of the catalyst from a product, catalyst recovery and recovery of the molar ratio of the catalyst (AHF supplementation). Although this process scheme allows for the recovery of the molar ratio of AHF to amine in the AHF-amine catalyst system, a portion of the amine is lost during the catalyst to product separation process before the AHF is replenished. Before the catalyst and the reaction product are separated, the AHF ratio in the AHF-amine catalyst system is restored to the state before reaction, thereby preventing the amine in the AHF-amine catalyst system from being lost after being decomposed into monomers, fundamentally solving the problem of the maladjustment of the molar ratio of the AHF to the amine in the AHF-amine catalyst system, prolonging the service cycle of the catalyst, and reducing the cost of finished products and solid waste disposal.
The equipment is improved: the main equipment of the existing process flow comprises a catalyst reaction kettle (function: synthesis and recovery of catalyst, and AHF replenishment), an F227 reactor (function: synthesis of F227 in catalyst), and a distillation tower (function: separation of catalyst and product). By adopting the method, the function of the existing equipment needs to be changed, the catalyst reaction kettle only needs to keep the catalyst synthesis function, the F227 reactor is added with the functions of catalyst recovery and AHF replenishment on the basis of the existing function, and the function of the distillation tower is not changed. Therefore, the main device to be modified in the present invention is the F227 reactor, and since the function of the F227 reactor is to react HFP in a catalyst system to produce F227 (heptafluoropropane), the reactor is only provided with a catalyst feed port and an HFP feed port, so that an AHF feed port needs to be added to the F227 reactor.
According to the invention, AHF is supplemented before the catalyst and heptafluoropropane (F227) are separated, so that the standard molar ratio of a catalyst reactor is recovered, the amine monomer can be effectively prevented from being decomposed by the catalyst, the molar ratio of AHF to amine in an AHF-amine catalyst system is not disordered, the catalyst is not invalid, and the service cycle of the catalyst can be effectively prolonged. Triethylamine hydrogen fluoride is the main component of the catalyst in an AHF-amine catalyst system, the molar ratio of AHF to triethylamine in the triethylamine hydrogen fluoride can be 1:1, 2:1, 3:1 and 4:1, when the molar ratio is reduced to be below 2:1, the triethylamine hydrogen fluoride can generate crystallization separation in an n-butyl alcohol solvent, and obvious amine odor is emitted, which indicates that part of triethylamine is already decomposed; when the molar ratio is higher than 2:1, triethylamine hydrogen fluoride is liquid and has no amine odor, indicating that triethylamine is not decomposed. Triethylamine has a flash point of-7 ℃ and strong volatility, and is easy to be entrained and lost in an F227 device system. Therefore, the decomposition of triethylamine is reduced, and the loss of triethylamine can be effectively reduced.
Detailed Description
(1) Preparing the catalyst in a catalyst reaction kettle to form an AHF-amine catalyst system.
The catalyst system consists of AHF (anhydrous hydrogen fluoride), triethylamine and n-butanol, wherein salt generated by the reaction of the AHF and the triethylamine is the main component of the catalyst, and the n-butanol is the solvent of the catalyst. The molar ratio of AHF to triethylamine is controlled to be 2.5:1, and the mass ratio of triethylamine hydrogen fluoride to n-butanol is controlled to be 2.1: 1. The feeding sequence is that firstly, n-butyl alcohol is fed into a catalyst reaction kettle at one time, then triethylamine is fed into a catalyst reaction kettle at one time, after stirring and mixing are carried out uniformly, AHF is fed into the catalyst reaction kettle at the flow rate of 60-70 kg/h, the temperature of the catalyst reaction kettle is controlled to be 50-60 ℃, the pressure is controlled to be 0.05-0.1 MPa, and after the feeding is finished, stirring is carried out for 30min, and then the reaction is completed.
(2) Feeding the prepared catalyst into a heptafluoropropane reactor at one time, feeding hexafluoropropylene into the heptafluoropropane reactor at a flow rate of 400-500 kg/h, controlling the temperature of the reactor to be 50-65 ℃, controlling the pressure to be 0.15-0.3 MPa, and synthesizing the heptafluoropropane by using the hexafluoropropylene and AHF in the catalyst in a molar ratio of 1: 1.
(3) After completion of the heptafluoropropane synthesis, the AHF in the catalyst has been partially consumed, for example, 1050kg of hexafluoropropene may be fed to consume 140kg of hydrogen fluoride, and 140kg of additional hydrogen fluoride may be fed to the heptafluoropropane reactor to restore the molar ratio of AHF to amine in the catalyst.
When the AHF is supplemented, feeding the AHF into a heptafluoropropane reactor at a flow rate of 60-70 kg/h, controlling the temperature of the reactor to be 50-65 ℃ and controlling the pressure to be 0.15-0.3 MPa.
(4) And after the AHF feeding is finished and the reaction is completed, feeding the mixed material of the catalyst and the heptafluoropropane into a distillation tower for separation. The temperature of the distillation tower kettle is controlled to be 60-65 ℃, the top temperature is controlled to be 10-20 ℃, the pressure is controlled to be 0.05-0.15 MPa, and the catalyst and the heptafluoropropane can be separated.
(5) And (4) recovering the catalyst. And (3) completing crude distillation when the pressure in the distillation tower is reduced to below 0.05MPa, feeding the crude gas F227 in the tower top into a downstream working section for purification, cooling the catalyst in the tower kettle to 45-50 ℃ by circulating water, and conveying the cooled catalyst into an F227 reactor by a centrifugal pump for next F227 synthesis.
The above embodiments do not limit the present invention in any way, and all technical solutions obtained by means of equivalent substitution or equivalent transformation fall within the protection scope of the present invention.
Claims (6)
1. The method for prolonging the service cycle of the catalyst for synthesizing the heptafluoropropane is characterized by comprising the following steps of:
(1) preparing a catalyst in a catalyst reaction kettle to form an AHF-amine catalyst system;
(2) adding a catalyst into a heptafluoropropane reactor, and introducing hexafluoropropylene into the heptafluoropropane reactor to synthesize heptafluoropropane;
(3) after the heptafluoropropane is synthesized, replenishing the consumed hydrogen fluoride in a heptafluoropropane reactor to restore the molar ratio of AHF to amine in the catalyst;
(4) after the AHF feeding is finished and the reaction is completed, feeding the mixed material of the catalyst and the heptafluoropropane into a distillation tower for separation;
(5) and (4) recovering the catalyst.
2. The method for prolonging the service life of the catalyst for synthesizing heptafluoropropane as claimed in claim 1, wherein in the step (1), said catalyst system comprises AHF, triethylamine and n-butanol, wherein a salt produced by the reaction of AHF and triethylamine is a main component of the catalyst, and n-butanol is a solvent of the catalyst; the molar ratio of AHF to triethylamine is 2.5:1, and the mass ratio of triethylamine hydrogen fluoride to n-butanol is 2.1: 1; the feeding sequence is as follows: firstly, once feeding n-butyl alcohol into a catalyst reaction kettle, once feeding triethylamine into a catalyst reaction kettle, uniformly stirring and mixing, then feeding AHF into the catalyst reaction kettle at a flow rate of 60-70 kg/h, controlling the temperature of the catalyst reaction kettle to be 50-60 ℃ and the pressure to be 0.05-0.1 MPa, and continuously stirring for 30min after feeding is finished, thus completing the reaction.
3. The method for prolonging the service life of a catalyst for synthesizing heptafluoropropane as claimed in claim 1, wherein in step (2), the prepared catalyst is fed into a heptafluoropropane reactor at a time, hexafluoropropylene is fed into the heptafluoropropane reactor at a flow rate of 400 to 500kg/h, the reactor temperature is controlled to 50 to 65 ℃, the pressure is controlled to 0.15 to 0.3MPa, and the molar ratio of hexafluoropropylene to AHF in the catalyst is 1: 1.
4. The method for prolonging the service life of the catalyst for synthesizing heptafluoropropane as claimed in claim 1, wherein in step (3), AHF is fed at a flow rate of 60-70 kg/h and introduced into a heptafluoropropane reactor, the temperature of the reactor is controlled to be 50-65 ℃, and the pressure is controlled to be 0.15-0.3 MPa.
5. The method for prolonging the service life of the catalyst for synthesizing heptafluoropropane as claimed in claim 1, wherein in the step (4), the temperature of the distillation tower is controlled to be 60-65 ℃, the top temperature is controlled to be 10-20 ℃, and the pressure is controlled to be 0.05-0.15 MPa, and the catalyst is separated from heptafluoropropane.
6. The method for prolonging the service life of the catalyst for synthesizing the heptafluoropropane as claimed in claim 1, wherein in the step (5), the rough distillation is completed when the pressure in the distillation tower is reduced to below 0.05MPa, the crude heptafluoropropane gas at the tower top enters a downstream section for purification, and the catalyst at the tower bottom is cooled to 45-50 ℃ by circulating water and then is conveyed into a heptafluoropropane reactor by a centrifugal pump for the next F227 synthesis.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911118665.1A CN110787836A (en) | 2019-11-15 | 2019-11-15 | Method for prolonging service cycle of catalyst for heptafluoropropane synthesis |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911118665.1A CN110787836A (en) | 2019-11-15 | 2019-11-15 | Method for prolonging service cycle of catalyst for heptafluoropropane synthesis |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110787836A true CN110787836A (en) | 2020-02-14 |
Family
ID=69444846
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911118665.1A Pending CN110787836A (en) | 2019-11-15 | 2019-11-15 | Method for prolonging service cycle of catalyst for heptafluoropropane synthesis |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110787836A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112500259A (en) * | 2020-12-14 | 2021-03-16 | 常熟三爱富中昊化工新材料有限公司 | Preparation method of heptafluoropropane |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1393431A (en) * | 2001-06-29 | 2003-01-29 | 常熟市中昊化工新材料研究所 | Process for preparing 2H-heptafluoropropane |
| CN1793094A (en) * | 2005-12-29 | 2006-06-28 | 浙江星腾化工有限公司 | Process for preparing pentafluoroethylane |
| CN101648873A (en) * | 2009-09-01 | 2010-02-17 | 中化国际（苏州）新材料研发有限公司 | Method for continuously preparing triethylamine hydrogen fluoride complex and reaction device thereof |
| CN101648872A (en) * | 2009-09-01 | 2010-02-17 | 中化国际（苏州）新材料研发有限公司 | Preparation method of triethylamine hydrogen fluoride complex |
| CN102786379A (en) * | 2012-08-30 | 2012-11-21 | 山东东岳高分子材料有限公司 | Production method for 1, 1, 1, 2, 3, 3, 3-heptafluoropropane |
| CN107021868A (en) * | 2013-03-12 | 2017-08-08 | 霍尼韦尔国际公司 | For reducing method of the 1233XF hydrofluorinations for 245CB formation during 244BB |
-
2019
- 2019-11-15 CN CN201911118665.1A patent/CN110787836A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1393431A (en) * | 2001-06-29 | 2003-01-29 | 常熟市中昊化工新材料研究所 | Process for preparing 2H-heptafluoropropane |
| CN1793094A (en) * | 2005-12-29 | 2006-06-28 | 浙江星腾化工有限公司 | Process for preparing pentafluoroethylane |
| CN101648873A (en) * | 2009-09-01 | 2010-02-17 | 中化国际（苏州）新材料研发有限公司 | Method for continuously preparing triethylamine hydrogen fluoride complex and reaction device thereof |
| CN101648872A (en) * | 2009-09-01 | 2010-02-17 | 中化国际（苏州）新材料研发有限公司 | Preparation method of triethylamine hydrogen fluoride complex |
| CN102786379A (en) * | 2012-08-30 | 2012-11-21 | 山东东岳高分子材料有限公司 | Production method for 1, 1, 1, 2, 3, 3, 3-heptafluoropropane |
| CN107021868A (en) * | 2013-03-12 | 2017-08-08 | 霍尼韦尔国际公司 | For reducing method of the 1233XF hydrofluorinations for 245CB formation during 244BB |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112500259A (en) * | 2020-12-14 | 2021-03-16 | 常熟三爱富中昊化工新材料有限公司 | Preparation method of heptafluoropropane |
| CN112500259B (en) * | 2020-12-14 | 2023-09-22 | 常熟三爱富中昊化工新材料有限公司 | Process for the preparation of heptafluoropropane |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR101310409B1 (en) | Process for preparing cyclohexanone and cyclohexanol | |
| JP2002518369A (en) | Post-treatment of distillation residue generated in the synthesis of tolylene diisocyanate | |
| CN100413786C (en) | Process for treating hydrazine hydrate waste salt water by ketone linking nitrogen method | |
| CN111454135A (en) | Device and process for preparing high-concentration methylal | |
| CN110787836A (en) | Method for prolonging service cycle of catalyst for heptafluoropropane synthesis | |
| US8481764B2 (en) | Process for producing propylene oxide | |
| CN108726483B (en) | Chlorine-containing tail gas recovery treatment method | |
| CN109809959A (en) | A kind of preparation method of 1,1,1,2,3- pentachloropropane | |
| CN112500259B (en) | Process for the preparation of heptafluoropropane | |
| KR101773588B1 (en) | Method for preparing o-chlorotoluene and p-chlorotoluene | |
| US5401873A (en) | Preparation of methyl formate | |
| JP5069222B2 (en) | Method for concentrating an aqueous ammonium carbamate stream | |
| CN108863717B (en) | Method for efficiently preparing alkynol | |
| CN101671274A (en) | Method for recycling phosgene in continuous production process of toluene di-isocyanate | |
| CN108530301A (en) | A kind of synthetic method of tri- fluorin benzyl amines of 2,4,6- | |
| JP2002173471A (en) | Method for splitting and collecting isocyanate-based to- be-split compound | |
| CN109468658B (en) | Preparation method of carbonyl fluoride | |
| US20120238782A1 (en) | Methods for producing allyl chloride and dichlorohydrin | |
| CN110950757B (en) | Production method and system of malonic diester | |
| US5453546A (en) | Method for the production of β-ionone from pseudoionone | |
| CN107108447B (en) | Steam stripping process | |
| JP2002544248A (en) | Production of 1,1,1,2,3,3,3-heptafluoropropane | |
| CN116496138B (en) | Preparation method and preparation device system of monofluoromethane | |
| CN115850211B (en) | Process method for synthesizing and co-producing acetamidine hydrochloride by using alpha-chloro-alpha-acetyl-gamma-butyrolactone and application thereof | |
| WO1999008998A1 (en) | Process for producing formamide |
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 | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20200214 |