CN205095746U - A high -efficient deamination apparatus for producing that is used for third / ethylene in urea synthesis carbonic acid ester - Google Patents
A high -efficient deamination apparatus for producing that is used for third / ethylene in urea synthesis carbonic acid ester Download PDFInfo
- Publication number
- CN205095746U CN205095746U CN201520892904.XU CN201520892904U CN205095746U CN 205095746 U CN205095746 U CN 205095746U CN 201520892904 U CN201520892904 U CN 201520892904U CN 205095746 U CN205095746 U CN 205095746U
- Authority
- CN
- China
- Prior art keywords
- cooling
- carbonic acid
- liquid
- vinyl acetate
- cushion chamber
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model provides a high -efficient deamination apparatus for producing that is used for third / ethylene in urea synthesis carbonic acid ester, the upper end of reation kettle body is equipped with the cooling tower, including the heat exchanger, rectifying section, liquid trap and the gaseous phase cushion chamber that from top to bottom connect gradually in the cooling tower, the rectifying section includes upper and lower regular packing layer and cooling layer, and the diameter on cooling layer is the 50% -90% of upper and lower regular packing layer diameter, and the cooling layer goes up to distribute there is cooling coil, the bottom on regular packing layer under in is installed to the liquid trap, the gaseous phase cushion chamber of liquid trap below is linked together with the reation kettle body, locate to be fixed with in this internal axis of rotation of reation kettle and get rid of the liquid dish, the inside of gaseous phase cushion chamber is equipped with the downspout, and the downspout upper end links to each other with the liquid outlet of liquid trap, and the lower extreme of downspout extends to through the reation kettle body and gets rid of liquid dish top. The utility model discloses simple structure, thus improve ammonia desorption efficiency and improved ureal conversion rate and third / ethylene in carbonic acid ester productivity, simultaneously, catalyst knot wall has effectively been prevented.
Description
Technical field
The utility model relates to a kind of chemical reaction device, especially a kind of high-efficient deamination process units for urea synthesizing carbonic acid third/vinyl acetate.
Background technology
Propene carbonate and ethylene carbonate are the polar organic solvents of function admirable, are also very important organic chemicals.They are widely used in the industrial circle such as natural gas purification, hydrogen manufacturing as high-efficiency desulfurization, decarbonization solvent; As a kind of intensive polar solvent, be the good solvent of the things hard to tolerate such as a kind of extracting petroleum distillate, raw lacquer, plasticizer, battery industry can be used as the fine solvent of lithium battery electrolytes.In recent years, utilize carbonic acid third/vinyl acetate and methyl alcohol ester exchange to produce the technique of dimethyl carbonate constantly ripe, due to having many uses of dimethyl carbonate, demand is large, and this has also widened the purposes of carbonic acid third/vinyl acetate.
In recent years, the process route of alcoholysis of urea carbonate synthesis third/vinyl acetate is progressively ripe, and this method is raw materials used cheap and easy to get, is very competitive clean Non oil-based route.Alcoholysis of urea carbonate synthesis third/vinyl acetate technique can adopt traditional reactor batch equipment, also can apply continuous rectification apparatus.
Chinese utility model patent CN203540544U discloses a kind of from reverse-flow type propene carbonate reactor, be characterized in adding gas from cooling and reflux device on traditional reactor, proportioning and the product quality of raw material can be ensured, but gas phase separation effect is not described.Chinese utility model patent CN2873777 discloses the process units of urea and propane diols Synthesis of dimethyl carbonate, comprise reactor, condensation receiving system etc., its condensation receiving system comprises heat exchanger and reactor return channel, pipeline between reactor return channel liquid outlet to reactor entrance is provided with fluid-tight, can effectively reclaim gas phase lime set, but gas phase separation effect is not illustrated equally.
Chinese utility model patent CN203329395U discloses a kind of Depressor response rectifier unit producing propene carbonate for urea method, enter Depressor response tower after it is characterized in that raw material mixing and carry out reactive distillation, tower top removes the ammonia that reaction produces in time, the propene carbonate produced is from tower reactor extraction, realize the continuous prodution that urea method produces propene carbonate, but in this device tower reactor, propylene carbonate ester content is only about 25%, and separating-purifying is more difficult.
Summary of the invention
The purpose of this utility model is to provide the high-efficient deamination process units for urea synthesizing carbonic acid third/vinyl acetate that a kind of structure is simple, can prevent catalyst knot wall while high-efficient deamination.
The utility model solves the technical scheme that prior art problem adopts: a kind of high-efficient deamination process units for urea synthesizing carbonic acid third/vinyl acetate, comprise the reactor body that outside is provided with steam jacket, the intrinsic center of reactor is provided with turning cylinder, the upper end of turning cylinder is connected with the motor of reaction kettle body outside, and the lower end of turning cylinder is connected with the agitator bottom reaction kettle body; The upper end of described reactor body is provided with cooling tower; The top of cooling tower is provided with gaseous phase outlet, comprises the heat exchanger, rectifying section, liquid trap and the gas phase cushion chamber that connect successively in cooling tower from top to bottom; The cooling layer that described rectifying section comprises upper and lower structured filling material layer and is located between upper and lower structured filling material layer, the diameter of cooling layer is the 50%-90% of upper and lower structured filling material layer diameter, and cooling layer is distributed with cooling coil; Liquid trap is installed on the bottom of described lower structured filling material layer; Gas phase cushion chamber below liquid trap is connected with the gaseous phase outlet of described reactor body; Be located on the intrinsic turning cylinder of reactor and be fixed with liquid throwing plate; The inside of described gas phase cushion chamber is provided with downspout, and the upper end of downspout is connected with the liquid outlet of described liquid trap, and the lower end of downspout extends to the top of liquid throwing plate by the gaseous phase outlet of reactor body.
The lateral wall of described cooling coil is provided with fin, and this fin comprises middle part perpendicular to cooling coil and is fixedly connected on vertical fins on cooling coil lateral wall and is located at vertical fins two ends and outward-dipping oblique fin.
Described heat exchanger is vertical array tubular heat exchanger.
Described liquid trap is ramp type liquid header, and the gas phase channel area of ramp type liquid header is the 60%-95% of cooling tower maximum cross section area.
Metallic plate corrugated regular filler is equipped with in described upper and lower structured filling material layer.
Described cooling layer is provided with multilayer cooling coil.
The height of described gas phase cushion chamber is 0.5-2m.
The beneficial effects of the utility model are: the utility model structure is simple, by connecting a cooling tower comprising heat exchanger, rectifying section, liquid trap and gas phase cushion chamber on traditional carbonic acid third/vinyl acetate reactor body, improve ammonia removal efficiency thus improve conversion ratio and carbonic acid third/vinyl acetate productive rate of urea; Meanwhile, the phegma of cooling tower forms falling film evaporation section at still wall under the effect of liquid throwing plate, not only increases ammonia removal efficiency, and wall tied by effective catalyst that must prevent.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
Fig. 2 is the structural representation of the utility model rectifying section.
In figure: the gaseous phase outlet of structured filling material layer, 703-cooling layer, 704-cooling coil, 705-vertical fins, the oblique fin of 706-, 101-reactor body under 1-reactor body, 2-steam jacket, 3-turning cylinder, 4-motor, 5-agitator, 6-vertical array tubular heat exchanger, 7-rectifying section, 8-ramp type liquid header, 9-gas phase cushion chamber, 10-liquid throwing plate, 11-downspout, the upper structured filling material layer of 701-, 702-.
Detailed description of the invention
Below in conjunction with the drawings and the specific embodiments, the utility model is described:
Fig. 1 is the structural representation of a kind of high-efficient deamination process units for urea synthesizing carbonic acid third/vinyl acetate of the utility model.A kind of high-efficient deamination process units for urea synthesizing carbonic acid third/vinyl acetate, comprise reactor body 1, steam jacket 2 is provided with outside it, center in reactor body 1 is provided with turning cylinder 3, the upper end of turning cylinder 3 is connected with the motor 4 being arranged at reaction kettle body 1 outside, and the lower end of turning cylinder 3 is fixedly connected with the agitator 5 bottom reaction kettle body 1; Cooling tower is provided with in the upper end of reactor body 1; The top of this cooling tower is provided with gaseous phase outlet, comprises the heat exchanger (preferred vertical array tubular heat exchanger 6), rectifying section 7, liquid trap (preferred ramp type liquid header 8) and the gas phase cushion chamber 9 that connect successively in this cooling tower from top to bottom.
Fig. 2 is the structural representation of rectifying section of the present utility model.As shown in Figure 2, the cooling layer 703 that rectifying section comprises structured filling material layer 701, lower structured filling material layer 702 and is located between structured filling material layer 701, lower structured filling material layer 702, is preferably equipped with metallic plate corrugated regular filler in upper structured filling material layer 701, lower structured filling material layer 702.Usually upper structured filling material layer 701 has identical diameter with lower structured filling material layer 702.The diameter of cooling layer 703 is upper structured filling material layer 701(or lower structured filling material layer 702) 50%-90% of diameter.Reducing of cooling layer 703 diameter can increase the intersegmental gas of rectifying section, improves heat transfer efficiency, effectively reduces heat transfer area.Cooling layer 703 is provided with single or multiple lift cooling coil 704, to meet the requirement of shifting out heat, wherein employing arranges multilayer cooling coil 704 and realizes multi-stage condensing while guarantee air outlet temperature, can the temperature of raising lime set of amplitude peak, reduce the consumption of reactor heat energy, the ammonia content in lime set can be reduced simultaneously, promote separating effect, improve reaction rate to a certain extent.The lateral wall of every bar cooling coil 704 is provided with fin, this fin is by vertical fins 705 and be located at vertical fins 705 two ends and outward-dipping oblique fin 706 forms, wherein, the middle part of vertical fins 705 is fixedly connected on the lateral wall of cooling coil 704 perpendicular to cooling coil 704; Wherein, the oblique fin 706 be positioned at above cooling coil 704 plays the effect of distribution of gas and liquid collection; The oblique fin 706 be positioned at below cooling coil 706 can play the effect of distribution of gas and liquid distribution.Ramp type liquid header 8 is installed on the bottom of lower structured filling material layer 702 and makes the gas phase channel area of ramp type liquid header 8 account for the 60%-95% of cooling tower maximum cross section area; Be positioned at the gas phase cushion chamber 9 below ramp type liquid header 8 to be connected with the gaseous phase outlet 101 of reactor body 1, the height of gas phase cushion chamber is preferably 0.5-2m; Be located on the turning cylinder 3 in reactor body 1 and be fixed with liquid throwing plate 10, usual liquid throwing plate 10 is arranged at the top in reactor body 1.The inside of gas phase cushion chamber 9 is provided with downspout 11, and the upper end of downspout 11 is connected with the liquid outlet of described ramp type liquid header 8, and the lower end of downspout 11 extends to the top of liquid throwing plate 10 by the gaseous phase outlet 101 of reactor body 1.
When utilizing the utility model to carry out the reaction of urea synthesizing carbonic acid third/vinyl acetate, need reactor body 1 of the present utility model to access in premixing system and filtration system, and to be connected with vacuum system by the gaseous phase outlet at cooling tower top and to pass into warm water in vertical array tubular heat exchanger 6 and cooling coil 704.Its concrete course of work is as follows:
(1), third (or second) glycol, urea and catalyst granules fully mix at premixing system, dissolve after, send in reactor body 1 by premixing system discharging pump;
(2) material, in reactor body 1 closes premixing system discharging pump after reaching and specifying liquid level, opens motor 4 and drives agitator 5 to stir, and start pumped vacuum systems.When vacuum in reactor body 1 reaches after reaction requirement, reaction temperature is warming up to certain heating rate, the ammonia that reaction produces and the gaseous phase outlet 101 that a small amount of material pushes up from reactor body 1 enter cooling tower, and through rectifying, condensation, ammonia is drawn into vacuum system; Its condensate liquid is collected by ramp type liquid header 8, be back on liquid throwing plate 10 through downspout 11 again, liquid throwing plate 10 under the action of the centrifugal, the inwall that phegma is evenly dispersed reactor body 1 declines along still wall film-like under neutrality effect, this section of still wall plays falling film evaporation effect, thus the ammonia dissolved in phegma is constantly distilled out of, ammonia removal efficiency is further enhanced, phegma cleans automatically to the top sidewall of reactor constantly simultaneously, effectively prevent catalyst knot wall;
(3), after the material in reactor reaction time reaches setting-up time, subsequent filter system is sent into by the discharging pump through reactor body 1.
Experiment proves, after propane diols, urea and catalyst (zinc oxide) being added premixing system by the mass ratio of 100:50:1, dissolves, being warming up to 55 DEG C, is squeezed in reactor body by premixing system discharging pump.Reactor body is 50kPa at pressure, and reaction temperature is 150 DEG C, and circulating fluid flow rate is 0.5m3/h, under the reaction condition of reaction time 2h.Analysis result shows, and can't detect urea content in reactant liquor after 2h, i.e. conversion rate of urea 100%, now propene carbonate yield is 97.5%, and the ammonia concentration at the gaseous phase outlet place of cooling tower is 98.5%.
Above content is in conjunction with concrete optimal technical scheme further detailed description of the utility model, can not assert that concrete enforcement of the present utility model is confined to these explanations.For the utility model person of an ordinary skill in the technical field, without departing from the concept of the premise utility, some simple deduction or replace can also be made, all should be considered as belonging to protection domain of the present utility model.
Claims (7)
1. the high-efficient deamination process units for urea synthesizing carbonic acid third/vinyl acetate, comprise the reactor body (1) that outside is provided with steam jacket (2), center in reactor body (1) is provided with turning cylinder (3), the upper end of turning cylinder (3) is connected with the motor (4) of reaction kettle body outside, and the lower end of turning cylinder (3) is connected with the agitator (5) bottom reaction kettle body; It is characterized in that, the upper end of described reactor body (1) is provided with cooling tower; The top of cooling tower is provided with gaseous phase outlet; The heat exchanger, rectifying section (7), liquid trap and the gas phase cushion chamber (9) that connect successively is comprised from top to bottom in cooling tower; The cooling layer (703) that described rectifying section (7) comprises upper and lower structured filling material layer (701,702) and is located between upper and lower structured filling material layer (701,702); The diameter of cooling layer (703) is the 50%-90% of upper and lower structured filling material layer (701,702) diameter, cooling layer (703) is distributed with cooling coil (704); Liquid trap is installed on the bottom of described lower structured filling material layer; Gas phase cushion chamber (9) below liquid trap is connected with the gaseous phase outlet (101) of described reactor body (1); Be located on the turning cylinder (3) in reactor body (1) and be fixed with liquid throwing plate (10); The inside of described gas phase cushion chamber (9) is provided with downspout (11), the upper end of downspout (11) is connected with the liquid outlet of described liquid trap, and the lower end of downspout (11) extends to the top of liquid throwing plate (10) by the gaseous phase outlet (101) of reactor body (1).
2. a kind of high-efficient deamination process units for urea synthesizing carbonic acid third/vinyl acetate according to claim 1, it is characterized in that, the lateral wall of described cooling coil (704) is provided with fin, and this fin comprises middle part perpendicular to cooling coil (704) and the vertical fins (705) be fixedly connected on cooling coil (704) lateral wall and be located at vertical fins (705) two ends and outward-dipping oblique fin (706).
3. a kind of high-efficient deamination process units for urea synthesizing carbonic acid third/vinyl acetate according to claim 1, is characterized in that, described heat exchanger is vertical array tubular heat exchanger (6).
4. a kind of high-efficient deamination process units for urea synthesizing carbonic acid third/vinyl acetate according to claim 1, it is characterized in that, described liquid trap is ramp type liquid header (8), and the gas phase channel area of ramp type liquid header (8) is the 60%-95% of cooling tower maximum cross section area.
5. a kind of high-efficient deamination process units for urea synthesizing carbonic acid third/vinyl acetate according to claim 1, is characterized in that, described upper and lower structured filling material layer is equipped with metallic plate corrugated regular filler in (701,702).
6. a kind of high-efficient deamination process units for urea synthesizing carbonic acid third/vinyl acetate according to claim 1, it is characterized in that, described cooling layer (703) is provided with multilayer cooling coil (704).
7. a kind of high-efficient deamination process units for urea synthesizing carbonic acid third/vinyl acetate according to claim 1, is characterized in that, the height of described gas phase cushion chamber (9) is 0.5-2m.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520892904.XU CN205095746U (en) | 2015-11-11 | 2015-11-11 | A high -efficient deamination apparatus for producing that is used for third / ethylene in urea synthesis carbonic acid ester |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520892904.XU CN205095746U (en) | 2015-11-11 | 2015-11-11 | A high -efficient deamination apparatus for producing that is used for third / ethylene in urea synthesis carbonic acid ester |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205095746U true CN205095746U (en) | 2016-03-23 |
Family
ID=55511558
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520892904.XU Active CN205095746U (en) | 2015-11-11 | 2015-11-11 | A high -efficient deamination apparatus for producing that is used for third / ethylene in urea synthesis carbonic acid ester |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205095746U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113996080A (en) * | 2021-12-31 | 2022-02-01 | 山东海科新源材料科技股份有限公司 | Chemical condenser and method for condensing and separating gas-phase product by using same |
-
2015
- 2015-11-11 CN CN201520892904.XU patent/CN205095746U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113996080A (en) * | 2021-12-31 | 2022-02-01 | 山东海科新源材料科技股份有限公司 | Chemical condenser and method for condensing and separating gas-phase product by using same |
| CN113996080B (en) * | 2021-12-31 | 2022-05-06 | 山东海科新源材料科技股份有限公司 | Chemical condenser and method for condensing and separating gas-phase product by using same |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105418447B (en) | A kind of DMAC rectifier units and process | |
| CN102936198B (en) | Produce the method for vinyl acetate | |
| CN104370698B (en) | The technique of a kind of infiltration evaporation-compression rectification integrated purification methylcarbonate and methyl alcohol | |
| CN102295564A (en) | Continuous production process for DOP (Dioctyl Phthalate) and used equipment | |
| CN102976894A (en) | Catalysis rectification process for isopropanol synthesis through transesterification method, and production equipment thereof | |
| CN102070417A (en) | Dimethoxym ethane catalytic distillation production process and production equipment thereof | |
| CN106631739A (en) | Crotonaldehyde reaction rectification production method and device based on solid alkali | |
| CN100465147C (en) | Fractionating tower for separating acrylic aldehyde from 3-hydroxypropionaldehyde solution | |
| CN102399133B (en) | Method for preparing cyclopentanol from cyclopentene through indirect hydration method | |
| CN205095746U (en) | A high -efficient deamination apparatus for producing that is used for third / ethylene in urea synthesis carbonic acid ester | |
| CN109748791B (en) | Energy-saving method for producing dimethyl adipate | |
| CN104788321B (en) | Recycling device and recycling technology of dimethylamine | |
| CN102875328B (en) | Catalyzing rectifying technology for synthesizing sec-butyl alcohol through ester exchange method and production equipment of catalyzing rectifying technology | |
| CN101961562B (en) | Rectification device | |
| CN205253071U (en) | Air -lift type circular current reactor | |
| CN108689839A (en) | A method of utilizing formic acid, acetate mixture production cyclohexyl formate and cyclohexyl acetate | |
| CN102225889A (en) | Method for preparing dimethyl ether by dehydration of methanol | |
| CN2903059Y (en) | Production apparatus of producing dimethyl ether by gas phase catalyzing methanol dehydrolysis | |
| CN105195064B (en) | Improved reaction separation synchronous reactor | |
| CN215609419U (en) | N-methyl diisopropanolamine continuous rectification device | |
| CN105457565B (en) | A kind of Airlift circulating reactor and the method that third/vinyl acetate of carbonic acid is prepared with it | |
| CN203938621U (en) | A kind of by the refining isobutyric suite of equipment of isobutyric aldehyde | |
| CN101245306B (en) | Method for producing white spirit base by recycling ethanol from waste yeast dried steam | |
| CN206204199U (en) | It is a kind of for urea/urea liquid and the reactor of polyols preparation cyclic organic carbonates | |
| CN208814917U (en) | A kind of formaldehyde reacts the catalytic rectifying tower for producing dimethoxym ethane with methanol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20200325 Address after: 047400 southeast of Nanjie Village, Yuwu Town, Tunliu County, Changzhi City, Shanxi Province Patentee after: Shanxi Zhongke Huian Chemical Co., Ltd Address before: 116039, D-1 building, spring garden, Ganjingzi District, Liaoning, Dalian Co-patentee before: Institute of Coal Chemistry, Chinese Academy of Sciences Patentee before: DALIAN CHEMICAL INSTITUTE Co.,Ltd. |
|
| TR01 | Transfer of patent right |