CN112159370A - Reaction system and method of CHPPO device - Google Patents
Reaction system and method of CHPPO device Download PDFInfo
- Publication number
- CN112159370A CN112159370A CN202010970528.7A CN202010970528A CN112159370A CN 112159370 A CN112159370 A CN 112159370A CN 202010970528 A CN202010970528 A CN 202010970528A CN 112159370 A CN112159370 A CN 112159370A
- Authority
- CN
- China
- Prior art keywords
- epoxidation
- reaction
- stage
- reactor
- propylene
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D301/00—Preparation of oxiranes
- C07D301/02—Synthesis of the oxirane ring
- C07D301/03—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds
- C07D301/19—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with organic hydroperoxides
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D303/00—Compounds containing three-membered rings having one oxygen atom as the only ring hetero atom
- C07D303/02—Compounds containing oxirane rings
- C07D303/04—Compounds containing oxirane rings containing only hydrogen and carbon atoms in addition to the ring oxygen atoms
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Epoxy Compounds (AREA)
Abstract
The invention relates to a reaction system and a reaction method of a CHPPO device, which mainly solve the problems of small production scale and high operation energy consumption in the prior art. By adopting the system and the method, in a CHPPO device with the production scale of 100-80 ten thousand tons/year, the propylene raw material and the reaction product at the outlet of the first-stage reaction logic 1-position reactor exchange heat, the heat exchange amount is 176.2-183.4 kilocalories/kg PO, the low-pressure steam required by propylene preheating is reduced, the circulating cooling water required by reaction product cooling is reduced, the low-pressure steam consumption is saved by 0.352-0.367 ton/ton PO, the circulating cooling water consumption is saved by 22.16-23.06 ton/ton PO, the problems are well solved, and the system and the method can be applied to the CHPPO device for producing propylene oxide.
Description
Technical Field
The invention relates to the field of PO production technology, in particular to a reaction system and a reaction method of a CHPPO device, which mainly comprise an epoxidation reaction process for generating propylene oxide PO and alpha, alpha-dimethyl benzyl alcohol DMBA by cumene hydroperoxide CHP and propylene and an energy optimization process for reacting propylene raw materials and exchanging heat of a reaction product at the outlet of a first-stage epoxidation reaction logic 1-bit reactor, and can be applied to the industrial production of preparing propylene oxide by a CHPPO method.
Background
Propylene oxide PO is one of three main derivatives of propylene, and is an important basic chemical raw material. More than 70% of propylene oxide is used to produce polyether polyols which are then reacted with isocyanates to synthesize polyurethanes. And the polyurethane is widely applied to the fields of automobiles, building heat preservation, refrigerators, elastic bodies, adhesives, coatings and the like.
At present, the industrial production method of propylene oxide PO mainly comprises chlorohydrin method CHPO, ethylbenzene co-oxidation method PO/SM, isobutane co-oxidation method PO/TBA, cumene oxidation method CHPPO, hydrogen peroxide direct oxidation method HPPO and oxygen direct oxidation method DOPO. The CHPO device adopting the chlorohydrination technology in domestic PO products accounts for about 50 percent of the total amount, and because the method can generate a large amount of calcium chloride waste residues and chlorine-containing waste water, the comprehensive treatment of the three wastes has large investment and high cost, and the current environment-friendly situation is severe, the environment-friendly supervision is frequently carried out in various places, once the excessive discharge causes the CHPO device to stop production and settle, and the shortage situation of the supply and demand of the PO market is caused.
Compared with the CHPO method which has serious pollution and the PO/SM and PO/TBA methods which have the defects of large investment, long flow path and more byproducts, the CHPPO method and the HPPO method have the advantages of competitive advantage of product cost and little environmental pollution; compared with HPPO method, CHPPO method has the advantages of almost no by-product in the whole process, lower three-waste discharge and safer operation, so that CHPPO method is expected to become the best process selection for PO production in the future. At present, the CHPPO process is mainly developed and mastered by Sumitomo chemical company of Sumitomo, Japan, only 12 million tons of CHPPO devices produced annually by Taishin Hongbaoli, Jiangsu, adopt the introduction method to produce PO products, and Chinese petrochemical company Limited has independently developed and completed a process package for preparing propylene oxide by 15 million tons of CHPPO annually and is prepared to be applied industrially in Tianjin petrochemical industry.
The invention discloses a method for preparing propylene oxide with patent application number CN201410429364.1 in the prior art, which discloses a method for removing trace acidic substances generated in the reaction process by contacting reaction materials with alkali-containing materials after epoxidation reaction of propylene and cumene hydroperoxide so as to reduce decomposition of the reaction materials, thereby improving the yield of Propylene Oxide (PO) products. The invention discloses a method for preparing propylene oxide with the patent application number of CN201480052389.2, which comprises the steps of dissolving propylene, hydrogen peroxide, acetonitrile and water in sylvite, then putting the materials into an epoxidation reactor containing a catalyst for epoxidation, and finally flowing out reaction materials containing propylene oxide, acetonitrile and water from the epoxidation reactor. The invention discloses a method for preparing propylene oxide by using a microchannel reactor with the patent application number of CN201611187680.8, and discloses a technical scheme that cumene hydroperoxide material and a catalyst are uniformly stirred at normal temperature to obtain a mixed solution, then the mixed solution and a propylene material are input into the microchannel reactor to react to obtain a crude product, and the crude product is separated and purified to obtain a target product.
However, the invention patent application No. CN201410429364.1 and the invention patent application No. CN201611187680.8 in the prior art are only laboratory scale processes, have the problem of "amplification effect", and cannot be directly applied to commercial industrial production devices, and the heating of the reaction raw materials and the cooling of the reaction products respectively need to consume steam and circulating cooling water, so that the energy is not comprehensively utilized. The invention patent application No. CN201480052389.2 is only a hydrogen peroxide method for producing propylene oxide, and has the problem of high operation risk in the preparation process of hydrogen peroxide raw materials. The CHPPO method for producing PO has the advantages of almost no discharge of byproducts and three wastes in the whole process, good operation safety and being the best process selection for producing PO in the future. Therefore, the 'amplification effect' in the epoxidation reaction process in the prior art is serious, the commercial industrial production is difficult, and process materials need to be heated and cooled repeatedly, so that a large amount of low-pressure steam and circulating cooling water are consumed; the problems of small production scale and large operation energy consumption exist.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a reaction system and a method of a CHPPO device, which mainly comprise an industrial reaction system of the CHPPO device and an energy optimization method, namely: the epoxidation reaction process of generating PO products and DMBA by-products by reacting CHP raw materials with propylene raw materials solves the blank problem of the domestic CHPPO process technology. Meanwhile, the epoxidation reaction energy is comprehensively utilized and optimized, the propylene raw material and the outlet reaction product of the first-stage epoxidation reaction logic 1-bit reactor are heated to the reaction temperature through low-pressure steam and enter the epoxidation reactor after heat exchange, and the outlet reaction product of the reactor is cooled through circulating cooling water after heat exchange, so that the problems that the propylene raw material needs a large amount of low-pressure steam for preheating, the outlet reaction product of the reactor needs a large amount of circulating cooling water for cooling and the like, and the energy utilization is unreasonable can be effectively solved.
In order to achieve the purpose, the invention adopts the following technical scheme:
the invention provides a reaction system of a CHPPO device, which comprises an epoxidation first-stage reaction unit, an epoxidation second-stage reaction unit, a propylene preheating heat exchange unit, a reaction product cooling unit and a propylene raw material heating unit in the CHPPO device with the production scale of 100 tons/year to 80 ten thousand tons/year;
wherein, the epoxidation first-stage reaction unit comprises m epoxidation first-stage reactors connected in series, and the epoxidation first-stage reactors are respectively epoxidation first-stage reaction logic 1-m reactors; the m series epoxidation first-stage reactors can be mutually switched, so that the activity of the catalyst in the series connected reactors is gradually improved from a logic 1-bit reactor to a logic m-bit reactor, and the epoxidation reaction is gradually deepened until a reaction product leaves the logic m-bit reactor;
the propylene preheating heat exchange unit comprises m propylene preheating heat exchangers which are respectively propylene preheating No. 1-m heat exchangers;
the reaction product cooling unit comprises m reaction product coolers, namely reaction product coolers from 1 to m;
the 1-m epoxidation first-stage reactors are sequentially connected with a corresponding propylene preheating heat exchanger and a corresponding reaction product cooler through pipelines;
the propylene raw material heating unit comprises 1 propylene raw material heater, and an inlet pipeline of the propylene raw material heater is connected with an outlet pipeline of the propylene preheating heat exchanger;
a propylene raw material feeding pipeline is connected with a propylene raw material inlet of the propylene preheating heat exchanger, and a propylene raw material outlet of the propylene preheating heat exchanger is sequentially connected with a propylene raw material heater and an epoxidation first-stage reaction logic 1-bit reactor through pipelines;
the epoxidation secondary reaction unit comprises n epoxidation secondary reactors connected in series, wherein the epoxidation secondary reactors are respectively epoxidation secondary reaction logic 1-n reactors;
the epoxidation first-stage reactor and the epoxidation second-stage reactor are connected in series through a pipeline, and the outlet of the m-number reaction product cooler is connected with the inlet of the epoxidation second-stage reaction logic 1-bit reactor through a pipeline.
Furthermore, the propylene raw material heater is communicated with a connecting pipeline of the epoxidation first-stage reaction logic 1-bit reactor and a cumene hydroperoxide CHP raw material pipeline.
The second aspect of the present invention provides a method based on the above reaction system, comprising the steps of:
firstly, Cumene Hydroperoxide (CHP) raw material and a reaction product flowing out of a logic 1-bit reactor of an epoxidation first-stage reaction exchange heat in a propylene preheating heat exchanger 1, and the propylene raw material heated in a propylene raw material heater by low-pressure steam is mixed and then enters the logic 1-bit reactor of the epoxidation first-stage reaction to generate epoxidation reaction;
after the reaction is finished, the reaction product flowing out of the bottom of the epoxidation first-stage reaction logic 1-bit reactor exchanges heat with a propylene raw material through a propylene preheating heat exchanger 1, is cooled through circulating cooling water of a reaction product cooler 1, and is sent into an epoxidation first-stage reaction logic 2-bit reactor to continue epoxidation; cooling the reaction product of the epoxidation first-stage reaction logic 2-bit reactor by circulating cooling water of a reaction product No. 2 cooler, and then sending the reaction product into an epoxidation first-stage reaction logic 3-bit reactor for continuously carrying out epoxidation reaction; repeating the steps until an m-bit reactor of the epoxidation first-stage reaction logic is obtained;
step three, cooling a reaction product flowing out of the m-bit reactor of the epoxidation first-stage reaction logic by circulating cooling water of a cooler for the reaction product m, and sequentially entering the epoxidation second-stage reaction logic 1-n-bit reactors to continue epoxidation until reaching the n-bit reactor of the epoxidation second-stage reaction logic;
and step four, sending the reaction product flowing out of the epoxidation second-stage reaction logic n-bit reactor to a high-pressure propylene recovery unit for rectification, separation and refining to finally obtain a PO product.
Furthermore, the epoxidation first-stage reactor and the epoxidation second-stage reactor are both adiabatic fixed bed reactors.
Further, the epoxidation primary reactors in the epoxidation primary reaction unit are connected in series and switchable; when the catalyst of the epoxidation first-stage reaction logic 1-bit reactor is invalid and the catalyst needs to be replaced, the original epoxidation first-stage reaction logic 2-bit reactor is switched to the epoxidation first-stage reaction logic 1-bit reactor, and so on until the original epoxidation first-stage reaction logic m-bit reactor, and the original epoxidation first-stage reaction logic 1-bit reactor after the catalyst is replaced is switched to the epoxidation first-stage reaction logic m-bit reactor.
Further, the operating temperature of the epoxidation first-stage reactor is 40-180 ℃, the operating pressure is 0.6-15.0 MPaA, and the molar ratio of the propylene raw material to the cumene hydroperoxide feed is 1-50: 1, the mass concentration of the cumene hydroperoxide feed is 2-95%, and the weight space velocity of the cumene hydroperoxide feed is 0.1-8.0 h-1The number of the epoxidation first-stage reactors connected in series is 1-10, the service life of the epoxidation first-stage reactor filled with the catalyst is 1-24 months, and the switching period of the epoxidation first-stage reactors is 0.5-12 months.
Further preferably, the operating temperature of the epoxidation first-stage reactor is 60-160 ℃, the operating pressure is 2.0-12.0 MPaA, and the molar ratio of the propylene raw material to the cumene hydroperoxide feed is 2-40: 1, the mass concentration of the cumene hydroperoxide feed is 4-90%, and the weight space velocity of the cumene hydroperoxide feed is 0.2-5.0 h-1The number of the epoxidation first-stage reactors connected in series is 2-8, the service life of the epoxidation first-stage reactor filled with the catalyst is 2-12 months, and the switching period of the epoxidation first-stage reactors is 1-9 months.
Furthermore, the operating temperature of the epoxidation secondary reactor is 40-180 ℃, the operating pressure is 0.1-12.0 MPaA, the number of the epoxidation secondary reactors connected in series is 1-10, and the service life of the catalyst filled in the epoxidation secondary reactor is 1-24 months.
More preferably, the operating temperature of the epoxidation secondary reactor is 60-160 ℃, the operating pressure is 1.0-10.0 MPaA, the number of the epoxidation secondary reactors connected in series is 2-8, and the service life of the catalyst filled in the epoxidation secondary reactor is 2-12 months.
By adopting the technical scheme, compared with the prior art, the invention has the following technical effects:
the invention relates to a reaction system and a method of a CHPPO device, wherein a propylene raw material and an outlet reaction product of an epoxidation first-stage reaction logic 1-bit reactor are preheated, heated to an epoxidation reaction temperature through low-pressure steam and then mixed with a CHP raw material to enter the logic 1-bit reactor for reaction, the reaction product is cooled by circulating cooling water after being used for heating the propylene raw material and is sent to a logic 2-bit reactor for further reaction, all reactors in the epoxidation first-stage reaction are in series operation, a logic last-stage reaction product is sent to an epoxidation second-stage reactor for reaction after being cooled by circulating water, the second-stage epoxidation reactor is also in series operation without switching, and all the first-stage epoxidation reactors and the second-stage epoxidation reactors in the system are adiabatic fixed bed reactors. The reaction product containing the PO preliminary product can be produced through the epoxidation process flow, and then the reaction product is sent to a high-pressure propylene recovery unit for rectification, separation and refining to finally obtain the PO product. Therefore, in the CHPPO device with the production scale of 100-80 ten thousand tons/year, the propylene raw material and the reaction product at the outlet of the epoxidation first-stage reaction logic 1-position reactor exchange heat, the heat exchange amount is 176.2-183.4 kilocalories/kilogram PO, the low-pressure steam consumption required by preheating the propylene raw material is reduced, meanwhile, the circulating cooling water consumption required by cooling the reaction product at the outlet of the epoxidation first-stage reactor logic 1-position reactor is reduced, the low-pressure steam consumption is saved by 0.352-0.367 tons/ton PO, the circulating cooling water consumption is reduced by 22.16-23.06 tons/ton PO, and a better technical effect is obtained.
Drawings
FIG. 1 is a reaction system and process flow for a CHPPO device of the present invention;
wherein, 1-cumene hydroperoxide CHP raw material; 2-propylene feed; 3-epoxidation first-stage reaction logic 1-bit reactor; 4-epoxidation first-stage reaction logic 2-bit reactor; a 3-bit reactor of 5-epoxidation first-stage reaction logic; 6-propylene preheat heat exchanger No. 1; 7-propylene preheat No. 2 heat exchanger; 8-propylene preheat No. 3 heat exchanger; 9-epoxidation second-stage reaction logic 1-bit reactor; a 10-epoxidation second-stage reaction logic 2-bit reactor; 11-epoxidation second-stage reaction logic 3-bit reactor; 12-reaction product No. 1 cooler; 13-reaction product No. 2 cooler; 14-reaction product No. 3 cooler; 15-propylene feed heater; 16-a reaction product;
taking an epoxidation first-stage reactor m-3 and an epoxidation second-stage reactor n-3 as examples, the reaction system and the method process flow of the invention patent CHPPO device are described as follows:
cumene hydroperoxide CHP raw material 1 from a cumene oxidation unit exchanges heat with a reaction product flowing out from a propylene preheating first-stage reaction logic 1-bit reactor in a propylene preheating heat exchanger 6, the propylene raw material 2 heated in a propylene raw material heater 15 by low-pressure steam is mixed and enters the top of an epoxidation first-stage reaction logic 1-bit reactor 3, epoxidation reaction is carried out in the epoxidation first-stage reaction logic 1-bit reactor 3, the reaction product obtained by the reaction flows out from the bottom of the epoxidation first-stage reaction logic 1-bit reactor 3, the propylene preheating first-stage heat exchanger 6 exchanges heat with the propylene raw material, the reaction product is cooled by circulating cooling water of a reaction product 1 cooler 12 and then is sent to the top of an epoxidation first-stage reaction logic 2-bit reactor 4, and epoxidation reaction is continuously carried out in the epoxidation first-stage reaction logic 2-bit reactor 4, the reaction product obtained by the reaction flows out from the bottom of the epoxidation first-stage reaction logic 2-bit reactor 4, is cooled by circulating cooling water of the reaction product No. 2 cooler 13, and then is sent to the top of the epoxidation first-stage reaction logic 3-bit reactor 5, the epoxidation reaction is continuously carried out in the epoxidation first-stage reaction logic 3-bit reactor 5, the reaction product obtained by the reaction flows out from the bottom of the epoxidation first-stage reaction logic 3-bit reactor 5, and is sent to the epoxidation second-stage reaction logic 1-bit reactor 9 after being cooled by circulating cooling water of the reaction product No. 3 cooler 14. And finally, conveying a reaction product 16 flowing out of the epoxidation second-stage reaction logic 3-bit reactor 11 to a high-pressure propylene recovery unit for rectification, separation and refining to finally obtain a PO product.
When the original epoxidation first-order reaction logic 1-bit reactor needs to be replaced due to catalyst deactivation, after the catalyst is replaced, the original epoxidation first-order reaction logic 2-bit reactor is switched to an epoxidation first-order reaction logic 1-bit reactor, the original epoxidation first-order reaction logic 3-bit reactor is switched to an epoxidation first-order reaction logic 2-bit reactor, and the original epoxidation first-order reaction logic 1-bit reactor after the catalyst is replaced is switched to an epoxidation first-order reaction logic 3-bit reactor. Cumene hydroperoxide CHP raw material 1 and propylene raw material 2 preheated by a propylene preheating heat exchanger No. 2 and heated by a propylene raw material heater 15 are mixed and then enter an epoxidation reaction of an epoxidation first-stage reaction logic 1-bit reactor, a reaction product obtained by the reaction flows out from the bottom of the epoxidation first-stage reaction logic 1-bit reactor, the heat exchange of the propylene preheating heat exchanger No. 2 and the propylene raw material 2 is carried out, the reaction product is cooled by circulating cooling water in a reaction product No. 2 cooler 13 and then sent into the epoxidation first-stage reaction logic 2-bit reactor for epoxidation reaction, the reaction product obtained by the reaction is sent into the epoxidation first-stage reaction logic 3-bit reactor for epoxidation reaction after being cooled by circulating cooling water in a reaction product No. 3 cooler 14, and the reaction product obtained by the reaction is cooled by circulating cooling water in a reaction product No. 1 cooler 12, feeding into a logic 1-bit reactor 9 of an epoxidation second-stage reaction, and the like. And finally, conveying a reaction product 16 flowing out of the epoxidation second-stage reaction logic 3-bit reactor 11 to a high-pressure propylene recovery unit for rectification, separation and refining to finally obtain a PO product.
Detailed Description
The invention provides a reaction system and a reaction method of a CHPPO device. The reaction system is arranged in a CHPPO device with the production scale of 100 tons/year to 80 ten thousand tons/year, and comprises an epoxidation first-stage reaction unit, an epoxidation second-stage reaction unit, a propylene preheating heat exchange unit, a reaction product cooling unit and a propylene raw material heating unit;
wherein, the epoxidation first-stage reaction unit comprises m epoxidation first-stage reactors connected in series, and the epoxidation first-stage reactors are respectively epoxidation first-stage reaction logic 1-m reactors; the m series epoxidation first-stage reactors can be mutually switched, so that the activity of the catalyst in the series connected reactors is gradually improved from a logic 1-bit reactor to a logic m-bit reactor, and the epoxidation reaction is gradually deepened until a reaction product leaves the logic m-bit reactor;
the propylene preheating heat exchange unit comprises m propylene preheating heat exchangers which are respectively propylene preheating No. 1-m heat exchangers;
the reaction product cooling unit comprises m reaction product coolers, namely reaction product coolers from 1 to m;
the 1-m epoxidation first-stage reactors are sequentially connected with a corresponding propylene preheating heat exchanger and a corresponding reaction product cooler through pipelines;
the propylene raw material heating unit comprises 1 propylene raw material heater, and an inlet pipeline of the propylene raw material heater is connected with an outlet pipeline of the propylene preheating heat exchanger;
a propylene raw material feeding pipeline is connected with a propylene raw material inlet of the propylene preheating heat exchanger, and a propylene raw material outlet of the propylene preheating heat exchanger is sequentially connected with a propylene raw material heater and an epoxidation first-stage reaction logic 1-bit reactor through pipelines;
the epoxidation secondary reaction unit comprises n epoxidation secondary reactors connected in series, and as the epoxidation reaction in the epoxidation secondary reactor enters the later stage, the reaction process is not violent any more, the reaction heat release is small, and the recovered energy is limited, a material heat exchange process is not set; the n epoxidation secondary reactors connected in series are epoxidation secondary reaction logic 1-n reactors respectively;
the epoxidation first-stage reactor and the epoxidation second-stage reactor are connected in series through a pipeline, and the outlet of the m-number reaction product cooler is connected with the inlet of the epoxidation second-stage reaction logic 1-bit reactor through a pipeline.
In a preferred embodiment of the present invention, the propylene raw material heater is connected with the connecting pipeline of the 1-position reactor of the epoxidation first-stage reaction logic and the cumene hydroperoxide CHP raw material pipeline.
The method based on the reaction system comprises the following steps:
firstly, Cumene Hydroperoxide (CHP) raw material and a reaction product flowing out of a logic 1-bit reactor of an epoxidation first-stage reaction exchange heat in a propylene preheating heat exchanger 1, and the propylene raw material heated in a propylene raw material heater by low-pressure steam is mixed and then enters the logic 1-bit reactor of the epoxidation first-stage reaction to generate epoxidation reaction;
after the reaction is finished, the reaction product flowing out of the bottom of the epoxidation first-stage reaction logic 1-bit reactor exchanges heat with a propylene raw material through a propylene preheating heat exchanger 1, is cooled through circulating cooling water of a reaction product cooler 1, and is sent into an epoxidation first-stage reaction logic 2-bit reactor to continue epoxidation; cooling the reaction product of the epoxidation first-stage reaction logic 2-bit reactor by circulating cooling water of a reaction product No. 2 cooler, sending the reaction product into an epoxidation first-stage reaction logic 3-bit reactor, and repeating the steps until the epoxidation first-stage reaction logic m-bit reactor is obtained; the propylene raw material is only subjected to heat exchange with the discharged material of the epoxidation first-stage reaction logic 1-bit reactor.
Step three, cooling a reaction product flowing out of the m-bit reactor of the epoxidation first-stage reaction logic by circulating cooling water of a cooler for the reaction product m, and sequentially entering the epoxidation second-stage reaction logic 1-n-bit reactors to continue epoxidation until reaching the n-bit reactor of the epoxidation second-stage reaction logic;
and step four, sending the reaction product flowing out of the epoxidation second-stage reaction logic n-bit reactor to a high-pressure propylene recovery unit for rectification, separation and refining to finally obtain a PO product.
Wherein, the epoxidation first-stage reactor in the epoxidation first-stage reaction unit is connected in series and can be switched; when the catalyst of the epoxidation first-stage reaction logic 1-bit reactor is invalid and the catalyst needs to be replaced, the original epoxidation first-stage reaction logic 2-bit reactor is switched to the epoxidation first-stage reaction logic 1-bit reactor, and so on until the original epoxidation first-stage reaction logic m-bit reactor, and the original epoxidation first-stage reaction logic 1-bit reactor after the catalyst is replaced is switched to the epoxidation first-stage reaction logic m-bit reactor. Thus, the activity of the catalyst in the reactors connected in series is gradually improved from the logic 1-bit reactor to the logic last-bit reactor, the reaction is gradually deepened until the reaction product leaves the logic last-bit reactor, and the reaction product is cooled by circulating cooling water and then is sent into an epoxidation second-stage reactor.
In a preferred embodiment of the present invention, all of the epoxidation first-stage reactors and all of the epoxidation second-stage reactors in the reaction system are adiabatic fixed bed reactors.
In a preferred embodiment of the present invention, the operating temperature of the epoxidation primary reactor is 40 to 180 ℃, the operating pressure is 0.6 to 15.0MPaA, and the molar ratio of the propylene raw material to the cumene hydroperoxide feed is 1 to 50: 1, the mass concentration of the cumene hydroperoxide feed is 2-95%, and the weight space velocity of the cumene hydroperoxide feed is 0.1-8.0 h-1The number of the epoxidation first-stage reactors connected in series is 1-10, the service life of the epoxidation first-stage reactor filled with the catalyst is 1-24 months, and the switching period of the epoxidation first-stage reactors is 0.5-12 months.
In a further preferred embodiment of the present invention, the operating temperature of the epoxidation first-stage reactor is 60 to 160 ℃, the operating pressure is 2.0 to 12.0MPaA, and the molar ratio of the propylene raw material to the cumene hydroperoxide feed is 2 to 40: 1, the mass concentration of the cumene hydroperoxide feed is 4-90%, and the weight space velocity of the cumene hydroperoxide feed is 0.2-5.0 h-1The number of the epoxidation first-stage reactors connected in series is 2-8, the service life of the epoxidation first-stage reactor filled with the catalyst is 2-12 months, and the switching period of the epoxidation first-stage reactors is 1-9 months.
In a preferred embodiment of the present invention, the operating temperature of the epoxidation secondary reactor is 40 to 180 ℃, the operating pressure is 0.1 to 12.0MPaA, the number of the epoxidation secondary reactors connected in series is 1 to 10, and the life of the catalyst filled in the epoxidation secondary reactor is 1 to 24 months.
In a further preferred embodiment of the present invention, the operating temperature of the epoxidation secondary reactor is 60 to 160 ℃, the operating pressure is 1.0 to 10.0MPaA, the number of the epoxidation secondary reactors connected in series is 2 to 8, and the life of the catalyst packed in the epoxidation secondary reactor is 2 to 12 months.
The present invention will be described in detail and specifically with reference to the following examples to facilitate better understanding of the present invention, but the following examples do not limit the scope of the present invention.
Comparative example 1
Taking a CHPPO industrial device with the production scale of 10 ten thousand tons/year as an example, the propylene oxide is produced by adopting the prior art, and a large amount of steam is consumed when the propylene raw material is heated to the reaction temperature by low-pressure steam; meanwhile, cooling of the reaction product by circulating cooling water requires consumption of a large amount of circulating cooling water. The consumption of low-pressure steam required for heating the propylene raw material was 6.33 tons/hr, and the consumption of circulating cooling water required for cooling the reaction product was 1372 tons/hr.
[ example 1 ]
By taking a CHPPO industrial device with the production scale of 10 ten thousand tons/year as an example, the reaction system and the method adopting the CHPPO device have the following brief process flow: preheating a propylene raw material and an outlet reaction product of an epoxidation first-stage reaction logic 1-bit reactor, heating the propylene raw material to an epoxidation reaction temperature through low-pressure steam, mixing the propylene raw material with a CHP raw material, allowing the mixture to enter the logic 1-bit reactor for reaction, cooling the reaction product by circulating cooling water after the propylene raw material is heated, allowing the cooled reaction product to enter the logic 2-bit reactor for further reaction, and repeating the steps. The technological operating parameters of the invention are as follows: the epoxidation first stage reactor was operated at 102 ℃ and 6.3MPaA, the molar ratio of propylene feed to cumene hydroperoxide feed was 12: 1, the mass concentration of the cumene hydroperoxide feed is 35 percent, and the weight space velocity of the cumene hydroperoxide feed is 3.2h-1The number of the epoxidation first-stage reactors connected in series is m-3, the temperature difference of the epoxidation first-stage reactors is 65.8 ℃, 44.8 ℃ and 23.8 ℃, the service life of the catalyst filled in the epoxidation first-stage reactor is 8 months, and the switching period of the epoxidation first-stage reactor is 4 months. The operation temperature of the epoxidation secondary reactor is 92 ℃, the operation pressure is 5.3MPaA, the number of the epoxidation secondary reactors connected in series is n-3, the temperature difference of the epoxidation secondary reactors is 53.2 ℃, 32.2 ℃ and 11.2 ℃, and the service life of the epoxidation secondary reactor filled with the catalyst is 8 months.
In a CHPPO industrial device with the production scale of 10 ten thousand tons/year, the technical scheme of the invention is adopted to carry out heat exchange on a propylene raw material and a reaction product at the outlet of a logic 1-bit reactor of an epoxidation first-stage reaction, and the heat exchange quantity is 2,245,000 kilocalories/hour; therefore, the low-pressure steam consumption required by preheating the propylene raw material is reduced, and meanwhile, the circulating cooling water consumption required by cooling the reaction product at the outlet of the logic 1-bit reactor of the epoxidation first-stage reactor is reduced; the consumption of low-pressure steam required for heating the propylene raw material is reduced to 1.85 tons/hour, and the consumption of circulating cooling water required for cooling the reaction product is reduced to 1089 tons/hour. Compared with the comparative example 1, the reaction unit of the CHPPO industrial device with 10 ten thousand tons/year saves 4.49 tons/hour of low-pressure steam and 282 tons/hour of circulating cooling water, and achieves better technical effect.
Comparative example 2
Taking a CHPPO industrial device with the production scale of 30 ten thousand tons/year as an example, the propylene oxide is produced by adopting the prior art, and a large amount of steam is consumed when the propylene raw material is heated to the reaction temperature by low-pressure steam; meanwhile, cooling of the reaction product by circulating cooling water requires consumption of a large amount of circulating cooling water. The consumption of low-pressure steam required for heating the propylene feed was 19.00 t/h, and the consumption of circulating cooling water required for cooling the reaction product was 4115 t/h.
[ example 2 ]
As in example 1, only the production scale and process operating parameters were changed to a 30-million ton/year CHPPO industrial plant with the following modifications of process operating parameters: the epoxidation first stage reactor was operated at 147 c, a pressure of 10.4MPaA, and a molar ratio of propylene feed to cumene hydroperoxide feed of 31: 1, the mass concentration of the cumene hydroperoxide feed is 56 percent, and the weight space velocity of the cumene hydroperoxide feed is 5.3h-1The number of the epoxidation first-stage reactors connected in series is m-4, the temperature difference of the epoxidation first-stage reactors is 68.1 ℃, 52.1 ℃, 36.1 ℃ and 20.1 ℃, the service life of the epoxidation first-stage reactor filled with the catalyst is 14 months, and the switching period of the epoxidation first-stage reactors is 8 months. The operating temperature of the epoxidation secondary reactor was 127 ℃, the operating pressure was 9.4MPaA, the number of epoxidation secondary reactors connected in series was 4, and the temperature differences of the epoxidation secondary reactors were 53.4 ℃, 39.4 ℃, 25.4 ℃, 11.4 ℃ respectivelyThe lifetime of the epoxidation secondary reactor packed with catalyst was 14 months.
In a CHPPO industrial device with the production scale of 30 ten thousand tons/year, the technical scheme of the invention is adopted to carry out heat exchange on the propylene raw material and the reaction product at the outlet of a logical 1-position reactor of the epoxidation first-stage reaction, the heat exchange amount is 6,753,750 kilocalories/hour, thereby the consumption of low-pressure steam required by heating the propylene raw material is reduced to 5.50 tons/hour, and the consumption of circulating cooling water required by cooling the reaction product is reduced to 3266 tons/hour. Compared with the comparative example 2, the reaction unit of the CHPPO industrial device of 30 ten thousand tons/year saves 13.50 tons/hour of low-pressure steam and 849 tons/hour of circulating cooling water, and achieves better technical effect.
Comparative example 3
Taking a CHPPO pilot plant with the production scale of 100 tons/year as an example, the propylene oxide is produced by adopting the prior art, and a large amount of steam is consumed when the propylene raw material is heated to the reaction temperature by low-pressure steam; meanwhile, cooling of the reaction product by circulating cooling water requires consumption of a large amount of circulating cooling water. The consumption of low-pressure steam required for heating the propylene feed was 6.33 kg/hr and the consumption of circulating cooling water required for cooling the reaction product was 1372 kg/hr.
[ example 3 ]
As in example 1, only the production scale and process operating parameters were changed to a 100 ton/year CHPPO pilot plant with the following modifications of process operating parameters: the number of the epoxidation first-stage reactors in series is m-1, the temperature difference of the epoxidation first-stage reactors is 45.8 ℃, the number of the epoxidation second-stage reactors in series is n-1, and the temperature difference of the epoxidation second-stage reactors is 33.2 ℃; the rest of the process operating parameters are unchanged.
In a CHPPO pilot-plant device with the production scale of 100 tons/year, the technical scheme of the invention is adopted to carry out heat exchange on a propylene raw material and a reaction product at the outlet of a logical 1-position reactor of an epoxidation first-stage reaction, the heat exchange amount is 2, 203 kilocalories/hour, so that the consumption of low-pressure steam required by heating the propylene raw material is reduced to 1.93 kilograms/hour, and the consumption of circulating cooling water required by cooling the reaction product is reduced to 1095 kilograms/hour. Compared with the comparative example 3, the reaction unit of the CHPPO pilot plant with 100 tons/year saves 4.40 kilograms/hour of low-pressure steam and 277 kilograms/hour of circulating cooling water, and achieves better technical effect.
Comparative example 4
Taking a CHPPO industrial device with the production scale of 80 ten thousand tons/year as an example, the propylene oxide is produced by adopting the prior art, and a large amount of steam is consumed when the propylene raw material is heated to the reaction temperature by low-pressure steam; meanwhile, cooling of the reaction product by circulating cooling water requires consumption of a large amount of circulating cooling water. The consumption of low-pressure steam required for heating the propylene raw material was 50.67 tons/hr, and the consumption of circulating cooling water required for cooling the reaction product was 10973 tons/hr.
[ example 4 ]
As in example 1, only the production scale and process operating parameters were changed to 80 million tons/year CHPPO industrial unit, with the process operating parameters modified as follows: the number of the epoxidation first-stage reactors in series is 10, the temperature difference of the epoxidation first-stage reactors is 67.5 ℃, 62.5 ℃, 57.5 ℃, 52.5 ℃, 47.5 ℃, 42.5 ℃, 37.5 ℃, 32.5 ℃, 27.5 ℃, 22.5 ℃, the number of the epoxidation second-stage reactors in series is 10, and the temperature difference of the epoxidation second-stage reactors is 49.3 ℃, 45.3 ℃, 41.3 ℃, 37.3 ℃, 33.3 ℃, 29.3 ℃, 25.3 ℃, 21.3 ℃, 17.3 ℃ and 13.3 ℃; the rest of the process operating parameters are unchanged.
In a CHPPO industrial device with the production scale of 80 ten thousand tons/year, the technical scheme of the invention is adopted to carry out heat exchange on the propylene raw material and the reaction product at the outlet of a logical 1-position reactor of the epoxidation first-stage reaction, the heat exchange quantity is 18,340,000 kilocalories/hour, so that the consumption of low-pressure steam required by heating the propylene raw material is reduced to 14.01 tons/hour, and the consumption of circulating cooling water required by cooling the reaction product is reduced to 8667 tons/hour. Compared with the comparative example 4, the reaction unit of the CHPPO industrial device of 80 ten thousand tons/year saves 36.66 tons/hour of low-pressure steam and 2306 tons/hour of circulating cooling water, and achieves better technical effect.
[ example 5 ]
In the same way [ example 2 ], the production scale was still the same, with only the process operating parameters being changed30 ten thousand tons per year CHPPO industrial device, the technological operation parameters are modified as follows: the epoxidation first stage reactor was operated at 40 ℃ and 0.6MPaA at a molar ratio of propylene feed to cumene hydroperoxide feed of 1: 1, the mass concentration of the cumene hydroperoxide feed is 2 percent, and the weight space velocity of the cumene hydroperoxide feed is 0.1h-1The number of the epoxidation first-stage reactors connected in series is 4, the temperature difference of the epoxidation first-stage reactors is 69.6 ℃, 52.6 ℃, 35.6 ℃ and 18.6 ℃, the service life of the epoxidation first-stage reactor filled with the catalyst is 24 months, and the switching period of the epoxidation first-stage reactors is 0.5 month. The operation temperature of the epoxidation secondary reactor is 40 ℃, the operation pressure is 0.1MPaA, the number of the epoxidation secondary reactors connected in series is 4, the temperature difference of the epoxidation secondary reactors is respectively 55.4 ℃, 40.4 ℃, 25.4 ℃ and 10.4 ℃, and the service life of the epoxidation secondary reactor filled with the catalyst is 24 months.
In a CHPPO industrial device with the production scale of 30 ten thousand tons/year, the technical scheme of the invention is adopted to carry out heat exchange on a propylene raw material and a reaction product at the outlet of a logical 1-bit reactor of an epoxidation first-stage reaction, the heat exchange amount is 6, 648 and 750 kilocalories/hour, so that the consumption of low-pressure steam required by heating the propylene raw material is reduced to 5.71 tons/hour, and the consumption of circulating cooling water required by cooling the reaction product is reduced to 3279 tons/hour. Compared with the comparative example 2, the reaction unit of the CHPPO industrial device of 30 ten thousand tons/year saves 13.29 tons/hour of low-pressure steam and 836 tons/hour of circulating cooling water, and achieves better technical effect.
[ example 6 ]
As in example 2, the production scale was still 30 million tons/year CHPPO industrial plant with only process operating parameters changed as follows: the epoxidation first stage reactor was operated at 180 ℃ and 15.0MPaA, with a molar ratio of propylene feed to cumene hydroperoxide feed of 50: 1, the mass concentration of the cumene hydroperoxide feed is 95 percent, and the weight space velocity of the cumene hydroperoxide feed is 8.0h-1The number of the epoxidation first-stage reactors connected in series is 4, and the temperature difference of the epoxidation first-stage reactors is 79.9 ℃, 62.9 ℃, 45.9 ℃ and 28 DEG respectively9 ℃, the service life of the catalyst filled in the epoxidation first-stage reactor is 1 month, and the switching period of the epoxidation first-stage reactor is 12 months. The operation temperature of the epoxidation secondary reactor is 180 ℃, the operation pressure is 12.0MPaA, the number of the epoxidation secondary reactors connected in series is 4, the temperature difference of the epoxidation secondary reactors is 65.0 ℃, 50.0 ℃, 35.0 ℃ and 20.0 ℃, and the service life of the epoxidation secondary reactor filled with the catalyst is 1 month.
In a CHPPO industrial device with the production scale of 30 ten thousand tons/year, the technical scheme of the invention is adopted to carry out heat exchange on the propylene raw material and the reaction product at the outlet of a logical 1-position reactor of the epoxidation first-stage reaction, the heat exchange amount is 6,690,000 kilocalories/hour, thereby the consumption of low-pressure steam required by heating the propylene raw material is reduced to 5.63 tons/hour, and the consumption of circulating cooling water required by cooling the reaction product is reduced to 3274 tons/hour. Compared with the comparative example 2, the reaction unit of the CHPPO industrial device of 30 ten thousand tons/year saves 13.37 tons/hour of low-pressure steam and 841 tons/hour of circulating cooling water, and achieves better technical effect.
The embodiments of the present invention have been described in detail, but the embodiments are merely examples, and the present invention is not limited to the embodiments described above. It will be appreciated by those skilled in the art that any equivalent modifications and substitutions are within the scope of the present invention. Accordingly, equivalent changes and modifications made without departing from the spirit and scope of the present invention should be covered by the present invention.
Claims (9)
1. A reaction system of a CHPPO device is characterized in that the CHPPO device with the production scale of 100 tons/year to 80 ten thousand tons/year comprises an epoxidation first-stage reaction unit, an epoxidation second-stage reaction unit, a propylene preheating heat exchange unit, a reaction product cooling unit and a propylene raw material heating unit;
the epoxidation first-stage reaction unit comprises m epoxidation first-stage reactors connected in series, wherein the epoxidation first-stage reactors are respectively epoxidation first-stage reaction logic 1-m reactors; the m series epoxidation first-stage reactors can be switched with each other, so that the activity of the catalyst in the series epoxidation reactors is gradually improved from a logic 1-bit reactor to a logic m-bit reactor, and the epoxidation reaction is gradually deepened until a reaction product leaves the logic m-bit reactor;
the propylene preheating heat exchange unit comprises m propylene preheating heat exchangers which are respectively propylene preheating No. 1-m heat exchangers;
the reaction product cooling unit comprises m reaction product coolers, namely reaction product coolers from 1 to m;
the 1-m epoxidation first-stage reactors are sequentially connected with a corresponding propylene preheating heat exchanger and a corresponding reaction product cooler through pipelines;
the propylene raw material heating unit comprises 1 propylene raw material heater, and an inlet pipeline of the propylene raw material heater is connected with an outlet pipeline of the propylene preheating heat exchanger;
a propylene raw material feeding pipeline is connected with a propylene raw material inlet of the propylene preheating heat exchanger, and a propylene raw material outlet of the propylene preheating heat exchanger is sequentially connected with a propylene raw material heater and an epoxidation first-stage reaction logic 1-bit reactor through pipelines;
the epoxidation secondary reaction unit comprises n epoxidation secondary reactors connected in series, and the epoxidation secondary reactors are respectively epoxidation secondary reaction logic 1-n reactors;
the outlet of the m-number reaction product cooler is connected with the inlet of the epoxidation second-stage reaction logic 1-bit reactor through a pipeline.
2. The reaction system of the CHPPO device as claimed in claim 1, wherein the propylene feed heater is connected to the connecting pipeline of the 1-position reactor of the epoxidation first-stage reaction logic and the CHP feed pipeline.
3. A method based on the reaction system as set forth in any one of claims 1 to 2, comprising the steps of:
firstly, Cumene Hydroperoxide (CHP) raw material and a reaction product flowing out of a first-stage epoxidation reaction logic 1-bit reactor exchange heat in a propylene preheating heat exchanger No. 1, and the propylene raw material heated in a propylene raw material heater by low-pressure steam is mixed and then enters the first-stage epoxidation reaction logic 1-bit reactor to carry out epoxidation reaction;
after the reaction is finished, the reaction product flowing out of the bottom of the epoxidation first-stage reaction logic 1-bit reactor exchanges heat with the propylene raw material through the propylene preheating heat exchanger No. 1, is cooled through circulating cooling water of a reaction product No. 1 cooler, and is sent into an epoxidation first-stage reaction logic 2-bit reactor to continue epoxidation; cooling the reaction product of the epoxidation first-stage reaction logic 2-bit reactor by circulating cooling water of a reaction product No. 2 cooler, and then sending the reaction product into an epoxidation first-stage reaction logic 3-bit reactor for continuously carrying out epoxidation reaction; repeating the steps until an m-bit reactor of the epoxidation first-stage reaction logic is obtained;
step three, cooling the reaction product flowing out of the m-bit reactor of the epoxidation first-stage reaction logic by circulating cooling water of a cooler for the reaction product m, and then sequentially entering the 1-n-bit reactors of the epoxidation second-stage reaction logic to continue the epoxidation reaction until reaching the n-bit reactor of the epoxidation second-stage reaction logic;
and step four, sending the reaction product flowing out of the epoxidation second-stage reaction logic n-bit reactor to a high-pressure propylene recovery unit for rectification, separation and refining to finally obtain a PO product.
4. The method of claim 3, wherein the epoxidation first stage reactor and the epoxidation second stage reactor are both adiabatic fixed bed reactors.
5. The method of claim 3, wherein the epoxidation first stage reactors in the epoxidation first stage reaction unit are connected in series and switchable; when the catalyst of the epoxidation first-stage reaction logic 1-bit reactor is invalid and the catalyst needs to be replaced, the original epoxidation first-stage reaction logic 2-bit reactor is switched to the epoxidation first-stage reaction logic 1-bit reactor, and so on until the original epoxidation first-stage reaction logic m-bit reactor, and the original epoxidation first-stage reaction logic 1-bit reactor after the catalyst is replaced is switched to the epoxidation first-stage reaction logic m-bit reactor.
6. The method of claim 3, wherein the epoxidation first stage reactor is operated at a temperature of 40 to 180 ℃ and at a pressure of 0.6 to 15.0MPaA, and wherein the molar ratio of the propylene feedstock to the cumene hydroperoxide feed is from 1 to 50: 1, the mass concentration of the cumene hydroperoxide feed is 2-95%, and the weight space velocity of the cumene hydroperoxide feed is 0.1-8.0 h-1The number of the epoxidation first-stage reactors connected in series is 1-10, the service life of a catalyst filled in the epoxidation first-stage reactor is 1-24 months, and the switching period of the epoxidation first-stage reactors is 0.5-12 months.
7. The method of claim 6, wherein the epoxidation first stage reactor is operated at a temperature of 60 to 160 ℃ and at a pressure of 2.0 to 12.0MPaA, and wherein the molar ratio of the propylene feedstock to the cumene hydroperoxide feed is 2 to 40: 1, the mass concentration of the cumene hydroperoxide feed is 4-90%, and the weight space velocity of the cumene hydroperoxide feed is 0.2-5.0 h-1The number of the epoxidation first-stage reactors connected in series is 2-8, the service life of the epoxidation first-stage reactor filled with a catalyst is 2-12 months, and the switching period of the epoxidation first-stage reactors is 1-9 months.
8. The method according to claim 3, wherein the operating temperature of the epoxidation secondary reactor is 40-180 ℃, the operating pressure is 0.1-12.0 MPaA, the number of the epoxidation secondary reactors connected in series is 1-10, and the service life of the catalyst filled in the epoxidation secondary reactor is 1-24 months.
9. The method according to claim 8, wherein the operating temperature of the epoxidation secondary reactor is 60-160 ℃, the operating pressure is 1.0-10.0 MPaA, the number of the epoxidation secondary reactors connected in series is 2-8, and the service life of the catalyst filled in the epoxidation secondary reactor is 2-12 months.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010970528.7A CN112159370A (en) | 2020-09-15 | 2020-09-15 | Reaction system and method of CHPPO device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010970528.7A CN112159370A (en) | 2020-09-15 | 2020-09-15 | Reaction system and method of CHPPO device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112159370A true CN112159370A (en) | 2021-01-01 |
Family
ID=73858556
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010970528.7A Pending CN112159370A (en) | 2020-09-15 | 2020-09-15 | Reaction system and method of CHPPO device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112159370A (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107286119A (en) * | 2016-04-12 | 2017-10-24 | 中国石油化工股份有限公司 | The process for purification of expoxy propane |
| CN107286118A (en) * | 2016-04-12 | 2017-10-24 | 中国石油化工股份有限公司 | The refining plant of expoxy propane |
| CN111097512A (en) * | 2018-10-25 | 2020-05-05 | 中国石油化工股份有限公司 | Process for preparing propylene oxide |
| CN112661585A (en) * | 2019-10-15 | 2021-04-16 | 中国石油化工股份有限公司 | Method for preparing isopropylbenzene by hydrogenolysis of alpha, alpha dimethyl benzyl alcohol and application |
-
2020
- 2020-09-15 CN CN202010970528.7A patent/CN112159370A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107286119A (en) * | 2016-04-12 | 2017-10-24 | 中国石油化工股份有限公司 | The process for purification of expoxy propane |
| CN107286118A (en) * | 2016-04-12 | 2017-10-24 | 中国石油化工股份有限公司 | The refining plant of expoxy propane |
| CN111097512A (en) * | 2018-10-25 | 2020-05-05 | 中国石油化工股份有限公司 | Process for preparing propylene oxide |
| CN112661585A (en) * | 2019-10-15 | 2021-04-16 | 中国石油化工股份有限公司 | Method for preparing isopropylbenzene by hydrogenolysis of alpha, alpha dimethyl benzyl alcohol and application |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US7141700B1 (en) | Decomposition of cumene hydroperoxide | |
| JP5628337B2 (en) | Process for the preparation of phenol from cumene | |
| KR102286147B1 (en) | Methanol Synthesis Process Layout for Mass Production Capacity | |
| CN103562179A (en) | High-yield process for the synthesis of urea | |
| CN103360265B (en) | Method for continuous hydrogenation of dinitrobenzene and recycling of reaction heat thereof | |
| CN112142689B (en) | Method and system for preparing cyclohexene oxide by using cyclohexene | |
| CN112159370A (en) | Reaction system and method of CHPPO device | |
| CN112279822A (en) | CHPPO device and method for improving yield of propylene oxide | |
| CN103709001A (en) | Method for producing glycol by ethylene oxide catalytic hydration | |
| CN109134217A (en) | Oxidation unit and oxidation technology improved method during a kind of cyclohexane oxidation process production cyclohexanone | |
| CN106608865A (en) | Energy-saving method for synthesizing ethylene carbonate | |
| CN101885712A (en) | Method for producing propylene oxide | |
| CN114380698B (en) | Method for synthesizing methylcyclohexanediamine by selective hydrogenation of diaminotoluene by continuous method | |
| CN109438167B (en) | Cyclohexene energy-saving production system and production method | |
| CN113527228B (en) | System and method for continuously producing propylene oxide by two-step methanol | |
| CN112125870A (en) | CHPPO device and method for optimizing epoxidation reaction system | |
| CN103708999A (en) | Method for producing glycol by catalytic hydration | |
| CN112191217B (en) | Continuous flow tubular reaction system and process for synthesizing adipic acid | |
| CN112239386B (en) | Process for producing ethylene by ethanol dehydration | |
| CN115304515B (en) | Preparation method of HDI biuret, combined production method and combined production device of HDI trimer and HDI biuret | |
| CN113512013B (en) | System and method for preparing propylene oxide from large-scale industrial methanol | |
| RU2472786C1 (en) | Method of producing propylene oxide | |
| CN116639699B (en) | Production process and system for preparing trichlorosilane | |
| CN111978206B (en) | Process system for synthesizing hexamethylene diamine key intermediate | |
| CN114835569B (en) | Method for producing photoinitiator UV-184 by condensation method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20210101 |