CN117924218A - Method for continuously producing epoxy chloropropane - Google Patents
Method for continuously producing epoxy chloropropane Download PDFInfo
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- CN117924218A CN117924218A CN202311864834.2A CN202311864834A CN117924218A CN 117924218 A CN117924218 A CN 117924218A CN 202311864834 A CN202311864834 A CN 202311864834A CN 117924218 A CN117924218 A CN 117924218A
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- Prior art keywords
- fixed bed
- bed reactor
- oil
- chloropropene
- epoxidation reaction
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- Pending
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- 238000000034 method Methods 0.000 title claims abstract description 38
- LRWZZZWJMFNZIK-UHFFFAOYSA-N 2-chloro-3-methyloxirane Chemical compound CC1OC1Cl LRWZZZWJMFNZIK-UHFFFAOYSA-N 0.000 title claims abstract description 12
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 51
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000003054 catalyst Substances 0.000 claims abstract description 31
- 238000006735 epoxidation reaction Methods 0.000 claims abstract description 31
- OWXJKYNZGFSVRC-NSCUHMNNSA-N (e)-1-chloroprop-1-ene Chemical compound C\C=C\Cl OWXJKYNZGFSVRC-NSCUHMNNSA-N 0.000 claims abstract description 23
- 238000000926 separation method Methods 0.000 claims abstract description 17
- 239000000463 material Substances 0.000 claims abstract description 11
- BRLQWZUYTZBJKN-UHFFFAOYSA-N Epichlorohydrin Chemical compound ClCC1CO1 BRLQWZUYTZBJKN-UHFFFAOYSA-N 0.000 claims description 31
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 19
- 230000008569 process Effects 0.000 claims description 15
- 239000002245 particle Substances 0.000 claims description 9
- 239000002808 molecular sieve Substances 0.000 claims description 8
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 8
- 238000010924 continuous production Methods 0.000 claims description 7
- 239000011259 mixed solution Substances 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 6
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 5
- 230000001172 regenerating effect Effects 0.000 claims description 5
- 229910052719 titanium Inorganic materials 0.000 claims description 5
- 239000010936 titanium Substances 0.000 claims description 5
- 230000001351 cycling effect Effects 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 238000007670 refining Methods 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 22
- 238000006243 chemical reaction Methods 0.000 abstract description 10
- 238000009776 industrial production Methods 0.000 abstract description 3
- 239000000047 product Substances 0.000 description 15
- 230000008929 regeneration Effects 0.000 description 9
- 238000011069 regeneration method Methods 0.000 description 9
- 239000006227 byproduct Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 3
- UGACIEPFGXRWCH-UHFFFAOYSA-N [Si].[Ti] Chemical compound [Si].[Ti] UGACIEPFGXRWCH-UHFFFAOYSA-N 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000005660 chlorination reaction Methods 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- XEPXTKKIWBPAEG-UHFFFAOYSA-N 1,1-dichloropropan-1-ol Chemical compound CCC(O)(Cl)Cl XEPXTKKIWBPAEG-UHFFFAOYSA-N 0.000 description 1
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- MLHOXUWWKVQEJB-UHFFFAOYSA-N Propyleneglycol diacetate Chemical compound CC(=O)OC(C)COC(C)=O MLHOXUWWKVQEJB-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 239000007809 chemical reaction catalyst Substances 0.000 description 1
- 150000003841 chloride salts Chemical class 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- XENVCRGQTABGKY-ZHACJKMWSA-N chlorohydrin Chemical compound CC#CC#CC#CC#C\C=C\C(Cl)CO XENVCRGQTABGKY-ZHACJKMWSA-N 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003822 epoxy resin Substances 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 239000004014 plasticizer Substances 0.000 description 1
- 229920000647 polyepoxide Polymers 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 150000003242 quaternary ammonium salts Chemical class 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000005060 rubber Substances 0.000 description 1
- 238000007127 saponification reaction Methods 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Classifications
-
- 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
- Epoxy Compounds (AREA)
Abstract
The invention belongs to the technical field of production of epoxy chloropropane, and in particular relates to a method for continuously producing epoxy chloropropane, which comprises the following steps of epoxidation reaction: feeding the preheated material into a fixed bed reactor for epoxidation reaction, and separating oil from water: sending the products separated from chloropropene and methanol into an oil-water separator for oil-water separation; the fixed bed reactor comprises a first fixed bed reactor and a second fixed bed reactor which are connected in parallel, and the oil-water separator comprises a plurality of oil-water separators which are connected in parallel. The method can ensure the stable reaction performance of the catalyst and the continuous and stable operation of the production process, thereby reducing the production cost, improving the production efficiency and meeting the requirement of the industrial production of the epoxy chloropropane.
Description
Technical Field
The invention belongs to the technical field of production of epichlorohydrin, and particularly relates to a method for continuously producing epichlorohydrin.
Background
The epoxy chloropropane is a chemical process raw material and an organic intermediate with extremely strong functionality, and is widely applied to the fields of epoxy resin, chlorohydrin rubber, plasticizer, ion exchange resin preparation and the like. At present, the method for preparing the epoxy chloropropane mainly comprises a propylene high-temperature chlorination method, a propylene acetate method, a glycerol chlorination method and a chloropropene direct epoxidation method. Wherein, the last step of the first three processes is dichloropropanol saponification reaction, which can produce a large amount of chlorine-containing wastewater and chloride salt waste residues.
The chloropropene direct epoxidation method using titanium-silicon molecular sieve as catalyst is used as the most potential green synthesis technology of epichlorohydrin, and has the advantages of low production energy consumption and environmental friendliness. Once the process is industrially applied, the process becomes a main object for producing transformation and becomes a main process for producing epichlorohydrin.
The chloropropene direct epoxidation method uses a fixed bed reactor in industrial production and has the advantages of high catalytic activity and selectivity, mild reaction conditions and the like. However, the catalyst is deactivated by accumulation of byproducts generated during the reaction, and when the catalytic activity of the catalyst is significantly reduced, a regeneration treatment is required, which is complicated and requires intermittent production stoppage. Meanwhile, the products after the reaction are subjected to oil-water separation, and intermittent production stopping is also required, and the processes directly affect the production efficiency and increase the running cost.
CN110698435A discloses a method for preparing epichlorohydrin, which uses a reaction bed as a reactor, chloropropene and hydrogen peroxide as raw materials, methanol as a solvent, a titanium silicalite molecular sieve as a catalyst, and quaternary ammonium salt as a surfactant. Although the service life of the titanium-silicon molecular sieve in the fixed bed is prolonged, the cycle period of the catalyst is prolonged, and the production efficiency is improved, the problems that intermittent production stopping, waste of reaction materials and large economic loss are required for the regeneration treatment of the catalyst and the subsequent oil-water separation cannot be avoided.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention provides a method for continuously producing epoxy chloropropane, which can ensure the stable reaction performance of a catalyst and the continuous and stable operation of a production process, thereby reducing the production cost and improving the production efficiency.
In order to achieve the above purpose, the invention adopts the following technical scheme:
a process for continuously producing epichlorohydrin comprising the steps of:
1) Mixing: the chloropropene and the methanol are sent into a mixer to be mixed uniformly, so as to prepare a mixed solution;
2) Preheating: feeding hydrogen peroxide and the mixed solution into a preheater, and preheating to a certain temperature;
3) Epoxidation reaction: feeding the preheated material into a fixed bed reactor for epoxidation reaction;
4) Cooling the product: sending the product after the epoxidation reaction into a cooler, and cooling to a certain temperature;
5) And (3) rectifying and separating: feeding the cooled product into a first rectifying tower for rectification, and separating chloropropene and methanol from the product;
6) Oil-water separation: sending the products separated from chloropropene and methanol into an oil-water separator for oil-water separation;
7) Refining epoxy chloropropane: feeding the separated oil phase into a second rectifying tower for rectification to obtain epichlorohydrin;
Wherein the fixed bed reactor comprises a first fixed bed reactor and a second fixed bed reactor which are connected in parallel, and the step 3) specifically comprises the following steps:
S1, feeding the preheated material into a first fixed bed reactor for epoxidation reaction; regenerating the catalyst in the second fixed bed reactor;
s2, feeding the preheated material into a second fixed bed reactor for epoxidation reaction; regenerating the catalyst in the first fixed bed reactor;
S3, repeatedly cycling the steps S1 to S2;
In the step 6), before the oil-water separation is completed, the product is sent to any one of the oil-water separators which are connected in parallel and not in operation, so as to implement the continuous oil-water separation process.
The invention adopts the first fixed bed reactor and the second fixed bed reactor which are connected in parallel, and can perform alternating epoxidation reaction and catalyst regeneration operation. When the first fixed bed reactor performs epoxidation reaction, the second fixed bed reactor performs catalyst regeneration; and when the first fixed bed reactor regenerates the catalyst, the second fixed bed reactor performs epoxidation reaction. The epoxidation reaction and the catalyst regeneration of the first fixed bed reactor and the second fixed bed reactor are operated alternately in a reciprocating manner, so that the catalyst is regenerated timely and effectively, the activity reduction caused by long-time operation of the catalyst and the intermittent production stopping of the production process are avoided effectively, the epoxidation reaction catalyst is always in a high-efficiency operation state, and the continuous high-efficiency production and high quality of the epichlorohydrin are ensured. Meanwhile, the invention adopts a plurality of parallel oil-water separators, and can be switched and used under the condition that a certain oil-water separator needs to stop production intermittently, so that the stability and reliability of equipment operation are improved, continuous operation in a separation stage is ensured, and the requirement of the full-flow continuous industrial production of epoxy chloropropane is met.
In the invention, the first fixed bed reactor and the second fixed bed reactor can be a plurality of fixed bed reactors connected in series and/or in parallel, and the reactor structures and the numbers of the first fixed bed reactor and the second fixed bed reactor are preferably the same so as to ensure the stability and the high efficiency of the reaction.
In the invention, the product of the epoxidation reaction comprises chloropropene, methanol, epichlorohydrin, water and byproducts, unreacted chloropropene and solvent methanol are separated sequentially through a first rectifying tower, water is separated through an oil-water separator, and byproducts are separated through a second rectifying tower, so that the high-purity epichlorohydrin is obtained.
Preferably, in step 1), the molar ratio of chloropropene to methanol is 1:5 to 20, more preferably 1:10 to 15.
Preferably, in step 2), the hydrogen peroxide is present in the form of a hydrogen peroxide solution having a mass concentration of 30 to 50%.
Preferably, in step 2), the molar ratio of the hydrogen peroxide to the chloropropene in the mixed solution is 1:0.5 to 5, more preferably 1:1 to 2.
Preferably, in step 2), the preheating is to 30℃to 60℃and more preferably to 35℃to 45 ℃.
Preferably, in step 3), the temperature of the epoxidation reaction is 30 to 60 ℃, more preferably 35 to 45 ℃.
Preferably, in step 3), the space velocity of the epoxidation reaction is from 0.2 to 50h -1, more preferably from 1 to 10h -1.
Preferably, in step 3), the fixed bed reactor is filled with a particle catalyst of titanium silicalite molecular sieve;
further preferably, the particle catalyst of the titanium silicalite molecular sieve has an MFI structure, and the particle size of the particles is 0.1mm to 10mm, more preferably 1mm to 3mm.
Preferably, in step 4), cooling is carried out to a temperature of from 10 ℃ to 30 ℃, more preferably to a temperature of from 15 ℃ to 25 ℃.
Preferably, in step 5), the method further comprises the steps of: the separated chloropropene and methanol are sent back to the mixer in the step 1) for recycling.
The invention has the advantages that:
According to the method for continuously producing epichlorohydrin, in the epoxidation reaction process, the first fixed bed reactor and the second fixed bed reactor which are used for alternately carrying out epoxidation reaction and catalyst regeneration are adopted for parallel operation, so that the problem that the catalyst needs to be stopped from being regenerated after being deactivated is solved; in the oil-water separation process, a plurality of oil-water separators are adopted for parallel operation, so that the problem that intermittent production stopping is required for oil-water separation is solved. Therefore, the production efficiency and the equipment use efficiency are improved, the method is suitable for industrial continuous production, the stability of the catalyst activity is ensured, and the method has the advantages of few byproducts, high epichlorohydrin selectivity and yield and the like.
Drawings
In order to more clearly illustrate the embodiments of the invention or the technical solutions in the prior art, the drawings that are needed in the description of the prior art in the embodiments are briefly described below, it being obvious that the drawings in the following description are some embodiments of the invention and that other drawings may be obtained from these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a flow chart of the process for continuously producing epichlorohydrin according to the invention.
Detailed Description
The present invention will be further described with reference to the accompanying drawings and detailed description, wherein it is to be understood that, on the premise of no conflict, the embodiments described below or technical features may be arbitrarily combined to form new embodiments.
Example 1
A process for the continuous production of epichlorohydrin, partially as shown in fig. 1, comprising the steps of:
1) Mixing: the chloropropene and the methanol are sent into a mixer in a molar ratio of 1:12 to be mixed uniformly, so as to prepare a mixed solution;
2) Preheating: feeding a hydrogen peroxide solution with the concentration of 30% and the mixed solution into a preheater, and preheating to 45 ℃; the molar ratio of the hydrogen peroxide to the chloropropene is 1:1.5;
3) Epoxidation reaction: feeding the preheated material into a fixed bed reactor for epoxidation reaction; the particle catalyst of titanium-silicon molecular sieve with MFI structure is filled in the fixed bed reactor, and the particle size of the particle is 1.2 mm-1.4 mm; the reaction temperature is controlled to be 45 ℃ by adopting constant-temperature circulating water; airspeed is 5h -1;
4) Cooling the product: the product after the epoxidation reaction is cooled to 25 ℃ by a cooler;
5) And (3) rectifying and separating: feeding the cooled product into a first rectifying tower for rectification, separating low-boiling chloropropene and methanol from the product, and returning the product to the step 1) for continuous participation in the reaction;
6) Oil-water separation: sending the product from which chloropropene and methanol are separated into an oil-water separator for liquid-liquid phase separation; the separated water phase is discharged as wastewater;
7) Refining epoxy chloropropane: delivering the separated oil phase into a second rectifying tower for rectification to obtain high-purity epichlorohydrin;
Wherein the fixed bed reactor comprises a first fixed bed reactor and a second fixed bed reactor which are connected in parallel, and the step 3) specifically comprises the following steps:
S1, feeding the preheated material into a first fixed bed reactor for epoxidation reaction for 100 hours; carrying out regeneration treatment on the catalyst in the second fixed bed reactor, wherein the regeneration treatment is specifically high-temperature roasting;
S2, feeding the preheated material into a second fixed bed reactor for epoxidation reaction for 100h; regenerating the catalyst in the first fixed bed reactor;
S3, repeatedly cycling the steps S1 to S2;
In the step 6), before the oil-water separation is completed, the product is sent to any one of the oil-water separators which are connected in parallel and not in operation, so as to implement the continuous oil-water separation process.
The method for continuously producing the epichlorohydrin of the example 1 is adopted, intermittent production stopping is not needed, meanwhile, the catalyst keeps high activity continuously, byproducts are few, the selectivity of the epichlorohydrin is stabilized at 95%, and the yield is stabilized at 90%.
Comparative example 1 (production of epichlorohydrin by comparative conventional method)
Comparative example 1 was conducted in a single fixed bed reactor, and as a result, after 100 hours of operation, the catalyst activity was greatly reduced, resulting in a decrease in epichlorohydrin selectivity of 90% or less, a decrease in epichlorohydrin yield of 80% or less, and a shutdown was required for catalyst regeneration.
The above examples are only illustrative of the preferred embodiments of the present invention and are not intended to limit the scope of the present invention, and various modifications and improvements made by those skilled in the art to the technical solution of the present invention should fall within the scope of protection defined by the claims of the present invention without departing from the spirit of the design of the present invention.
Claims (10)
1. A process for continuously producing epichlorohydrin comprising the steps of:
1) Mixing: the chloropropene and the methanol are sent into a mixer to be mixed uniformly, so as to prepare a mixed solution;
2) Preheating: feeding hydrogen peroxide and the mixed solution into a preheater, and preheating to a certain temperature;
3) Epoxidation reaction: feeding the preheated material into a fixed bed reactor for epoxidation reaction;
4) And (3) cooling: sending the product after the epoxidation reaction into a cooler, and cooling to a certain temperature;
5) And (3) rectifying and separating: feeding the cooled product into a first rectifying tower for rectification, and separating chloropropene and methanol from the product;
6) Oil-water separation: sending the products separated from chloropropene and methanol into an oil-water separator for oil-water separation;
7) Refining epoxy chloropropane: feeding the separated oil phase into a second rectifying tower for rectification to obtain epichlorohydrin;
Wherein the fixed bed reactor comprises a first fixed bed reactor and a second fixed bed reactor which are connected in parallel, and the step 3) specifically comprises the following steps:
S1, feeding the preheated material into a first fixed bed reactor for epoxidation reaction; regenerating the catalyst in the second fixed bed reactor;
s2, feeding the preheated material into a second fixed bed reactor for epoxidation reaction; regenerating the catalyst in the first fixed bed reactor;
S3, repeatedly cycling the steps S1 to S2;
In the step 6), before the oil-water separation is completed, the product is sent to any one of the oil-water separators which are connected in parallel and not in operation, so as to implement the continuous oil-water separation process.
2. The process for the continuous production of epichlorohydrin according to claim 1, characterized in that in step 1), the molar ratio of chloropropene to methanol is comprised between 1:5 and 20, preferably between 1:10 and 15.
3. The method for continuously producing epichlorohydrin according to claim 1 or 2, characterized in that in step 2), the hydrogen peroxide is present in the form of a hydrogen peroxide solution having a mass concentration of 30 to 50%.
4. A process for the continuous production of epichlorohydrin according to any of claims 1 to 3 characterized in that in step 2) the molar ratio of hydrogen peroxide to chloropropene in the mixture is from 1:0.5 to 5, preferably from 1:1 to 2.
5. The process for the continuous production of epichlorohydrin according to any of claims 1to 4, characterized in that in step 2) it is preheated to 30 ℃ to 60 ℃, preferably to 35 ℃ to 45 ℃.
6. The process for the continuous production of epichlorohydrin according to any of claims 1 to 5, characterized in that in step 3), the temperature of the epoxidation reaction is between 30 ℃ and 60 ℃, preferably between 35 ℃ and 45 ℃.
7. The method for continuously producing epichlorohydrin according to any of claims 1 to 6 characterized in that in step 3), the fixed bed reactor is filled with a particulate catalyst of titanium silicalite molecular sieve.
8. The method for continuously producing epichlorohydrin according to claim 7, characterized in that in step 3), the particle catalyst of the titanium silicalite molecular sieve has an MFI structure, and the particle size is 0.1mm to 10mm, preferably 1 to 3mm.
9. The process for the continuous production of epichlorohydrin according to any of claims 1to 8, characterized in that in step 4) it is cooled to 10 ℃ to 30 ℃, preferably to 15 ℃ to 25 ℃.
10. The method for continuously producing epichlorohydrin according to any of claims 1 to 9 characterized by further comprising, in step 5), the steps of: the separated chloropropene and methanol are sent back to the mixer in the step 1) for recycling.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311864834.2A CN117924218A (en) | 2023-12-29 | 2023-12-29 | Method for continuously producing epoxy chloropropane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311864834.2A CN117924218A (en) | 2023-12-29 | 2023-12-29 | Method for continuously producing epoxy chloropropane |
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| Publication Number | Publication Date |
|---|---|
| CN117924218A true CN117924218A (en) | 2024-04-26 |
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| CN202311864834.2A Pending CN117924218A (en) | 2023-12-29 | 2023-12-29 | Method for continuously producing epoxy chloropropane |
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- 2023-12-29 CN CN202311864834.2A patent/CN117924218A/en active Pending
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