CN204638162U - A kind of ethanol is around pipe synthesis reactor - Google Patents
A kind of ethanol is around pipe synthesis reactor Download PDFInfo
- Publication number
- CN204638162U CN204638162U CN201520219073.XU CN201520219073U CN204638162U CN 204638162 U CN204638162 U CN 204638162U CN 201520219073 U CN201520219073 U CN 201520219073U CN 204638162 U CN204638162 U CN 204638162U
- Authority
- CN
- China
- Prior art keywords
- reactor
- pipe
- reactor body
- around
- temperature receiver
- 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.)
- Withdrawn - After Issue
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model relates to a kind of ethanol around pipe synthesis reactor, comprise reactor body, material mixed gas inlet tube, syngas outlet pipe, go into operation electric heater, described material mixed gas inlet tube is positioned at the upside of reactor body, syngas outlet pipe is positioned at the downside of reactor body, material mixed gas inlet tube upper end connects the heater that goes into operation, it is characterized in that: be provided with heat exchange in described reactor body around pipe, described heat exchange is positioned on the downside of reactor body around the low-temperature receiver import of pipe, heat exchange is positioned on the upside of reactor around the low-temperature receiver outlet of pipe, described low-temperature receiver outlet is connected with the supporting useless pot of reactor.A kind of ethanol of the utility model has following beneficial effect around pipe synthesis reactor: 1, can reclaim the heat that reaction produces, recovered steam is for production system.2, ensure that the reaction temperature of bed, provide the stability of Dynamic System.3, the input of automatic control is reduced.
Description
Technical field
The present utility model relates to a kind of chemical industry synthesis reactor, relates to a kind of ethanol particularly around pipe synthesis reactor.
Background technology
Current conventional chemical industry synthesis reactor mainly contains following several: 1, tubular reactor; 2, tank reactor; 3, tower reactor; 4, fixed bed reactors; 5, fluidized-bed reactor; 6, moving-burden bed reactor.Wherein four kinds of mutually any anabolic reactions of reactor adapted gas, liquid, solid such as tank reactor, tower reactor, fluidized-bed reactor, moving-burden bed reactor.Gas, gas phase hybrid reaction generally adopt tubular fixed-bed reactor.Current synthesis reactor technology respectively has pluses and minuses: first is that power-saving technology and Environmental Safety measure are further improved; Second is that synthesis reactor medium trend needs to be optimized further, is beneficial to overall raising production Technology and running efficiency.
Summary of the invention
For the deficiency of above-mentioned synthesizing alcohol reactor technology, in conjunction with existing gas, gas synthesis reactor current development situation, the utility model provides a kind of ethanol around pipe synthesis reactor, uses automatic steam control temperature of reactor, heat recovery and utilization, improves the stability of operation.
A kind of ethanol is around pipe synthesis reactor, comprise reactor body, material mixed gas inlet tube, syngas outlet pipe, go into operation electric heater, described material mixed gas inlet tube is positioned at the upside of reactor body, syngas outlet pipe is positioned at the downside of reactor body, material mixed gas inlet tube upper end connects the heater that goes into operation, it is characterized in that: be provided with heat exchange in described reactor body around pipe, described heat exchange is positioned on the downside of reactor body around the low-temperature receiver import of pipe, heat exchange is positioned on the upside of reactor around the low-temperature receiver outlet of pipe, described low-temperature receiver outlet is connected with the supporting useless pot of reactor.
Described low-temperature receiver import is positioned at center on the downside of reactor body.
On the upside of described reactor body, both sides arrange low-temperature receiver outlet respectively.
On the downside of described reactor body, both sides arrange syngas outlet pipe respectively.
The lower end of described low-temperature receiver import is connected with boiler circulation pump.
The utility model ethanol is around pipe synthesis reactor, after material mixed gas is preheated by the electric heater that goes into operation, reactor body inside is entered on the upside of reactor body, namely reacting gas enters from upside, and downside goes out, and heat exchange is enter from downside around pipe, upside goes out, both traffic directions are contrary, thus can better reclaim the heat of reaction generation, and the intrinsic bed temperature of simultaneous reactions device is evenly distributed; Be connected to supporting useless pot from heat exchange around pipe steam out, can be used for resident living hot water.
On the downside of ethanol synthesis reactor body, center is provided with low-temperature receiver import, is convenient to water and evenly enters reactor.
Syngas outlet pipe is separately positioned on the both sides on the downside of synthesis reactor body, can uniform gas distribution.
On the upside of synthesis reactor body, both sides arrange low-temperature receiver outlet, and design can ensure that reactor temperature is evenly distributed like this, and gas arrives the supporting useless pot of reactor smoothly.
Low-temperature receiver of the present invention can be water, oil, air etc.
The utility model reacting appliance has following beneficial effect: 1, can reclaim the heat that reaction produces, recovered steam is for production system.2, ensure that the reaction temperature of bed, provide the stability of Dynamic System.3, the input of automatic control is reduced.
Accompanying drawing explanation
Fig. 1 is the structural representation of the utility model ethanol around pipe synthesis reactor.
In Fig. 1, each several part Reference numeral is respectively: 1: material mixed gas inlet tube, and 2: syngas outlet pipe, 3: syngas outlet pipe, 4: low-temperature receiver import, 5: low-temperature receiver exports, 6: low-temperature receiver exports, 7: the supporting useless pot of reactor, 8: boiler circulation pump, 9: go into operation electric heater, 10 reactor bodies, 11: heat exchange around pipe, 12: manhole and dumping pit.
Detailed description of the invention
As shown in Figure 1, the present invention proposes a kind of ethanol synthesis around pipe reactor.
A kind of ethanol is around pipe synthesis reactor, comprise the reactor body 10 of band manhole and dumping pit 12, heat exchange is around pipe 11, syngas outlet pipe 2, 3, material mixed gas inlet tube 1, go into operation electric heater 9, the supporting useless pot 7 of reactor, boiler circulation pump 8, low-temperature receiver import 4, low-temperature receiver outlet 5, 6, described material mixed gas inlet tube 1 is positioned at the upside of reactor body 10, syngas outlet pipe 2, 3 downsides being positioned at reactor body 10, material mixed gas inlet tube 1 upper end connects the heater 9 that goes into operation, heat exchange is provided with around pipe 11 in described reactor body 10, described heat exchange is positioned on the downside of reactor body 10 around the low-temperature receiver import 4 of pipe 11, the lower end of described low-temperature receiver import 4 is connected with boiler circulation pump 8, heat exchange is positioned on the upside of reactor around the low-temperature receiver outlet 5,6 of pipe 11, and described low-temperature receiver outlet 5,6 is connected with the supporting useless pot 7 of reactor.
The utility model reacting appliance has following beneficial effect: 1, can reclaim the heat that reaction produces, recovered steam is for production system.2, ensure that the reaction temperature of bed, provide the stability of Dynamic System.3, the input of automatic control is reduced.
Concrete operation flow process is as follows:
From hydrogen rich gas pressure ~ 3.7MPa, the temperature 40 DEG C of acetic acid hydrogenation process, first after inlet tower gas preheater preheats, enter vaporization tower from upper end.Raw material ethyl acetate pressure 3.9MPa, temperature 25 DEG C are sent into by the external world, first through ethyl ester preheater preheats to ~ 170 DEG C, sprayed into down in vaporizer by upper with mist by vaporization tower top atomizer, the hydrogen rich gas that vaporific ethyl acetate and top enter fully contacts through inner-tower filling material and gasifies, and finally goes out from the mouth of pipe bottom vaporization tower.Inlet tower gas preheater shell side, gone out the preheating of tower reaction gas from vaporization tower out synthesis gas, after reaching ethyl acetate activity of hydrocatalyst temperature, entered ethyl acetate hydrogenation reactor body.Above-mentioned tower air preheater, ethyl ester preheater, vaporization tower is also called the electric heater that goes into operation.
The gas entering reactor body carries out ethyl acetate hydrogenation reaction by catalyst layer from top to down, and by-product >=2.1MPa middle pressure steam.After reaction, gas goes out tower by bottom reactor body, then two heat exchangers after reactor are entered, by entering the unstripped gas of reactor outside the hot gas heating tube that reflects, the synthesis gas temperature of reactor is down to 90 DEG C, after enter one-level gas-liquid separator and carry out gas-liquid separation, after one-level is separated, gas goes cooler to be chilled to 50 DEG C, and wherein most second alcohol and water is condensed, then goes out coarse ethanol by secondary gas-liquid separator separates.
It should be noted that above-described embodiment is only for the utility model example is clearly described, and be not the restriction to embodiment of the present utility model.For those of ordinary skill in the field, other multi-form change or change can also be made on the basis of the above description.All within spirit of the present utility model and principle, any amendment made, equivalent replacement, improvement etc. are all included among protection domain of the present utility model.
Claims (5)
1. an ethanol is around pipe synthesis reactor, comprise reactor body, material mixed gas inlet tube, syngas outlet pipe, go into operation electric heater, described material mixed gas inlet tube is positioned at the upside of reactor body, syngas outlet pipe is positioned at the downside of reactor body, material mixed gas inlet tube upper end connects the heater that goes into operation, it is characterized in that: be provided with heat exchange in described reactor body around pipe, described heat exchange is positioned on the downside of reactor body around the low-temperature receiver import of pipe, heat exchange is positioned on the upside of reactor around the low-temperature receiver outlet of pipe, described low-temperature receiver outlet is connected with the supporting useless pot of reactor.
2. according to claim 1 around pipe reactor, it is characterized in that: described low-temperature receiver import is positioned at center on the downside of reactor body.
3. according to claim 1 around pipe reactor, it is characterized in that: on the upside of described reactor body, both sides arrange low-temperature receiver outlet respectively.
4. according to claim 1 around pipe reactor, it is characterized in that: on the downside of described reactor body, both sides arrange syngas outlet pipe respectively.
5. according to claim 1 around pipe reactor, it is characterized in that: the lower end of described low-temperature receiver import is connected with boiler circulation pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520219073.XU CN204638162U (en) | 2015-04-13 | 2015-04-13 | A kind of ethanol is around pipe synthesis reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520219073.XU CN204638162U (en) | 2015-04-13 | 2015-04-13 | A kind of ethanol is around pipe synthesis reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204638162U true CN204638162U (en) | 2015-09-16 |
Family
ID=54090938
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520219073.XU Withdrawn - After Issue CN204638162U (en) | 2015-04-13 | 2015-04-13 | A kind of ethanol is around pipe synthesis reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204638162U (en) |
-
2015
- 2015-04-13 CN CN201520219073.XU patent/CN204638162U/en not_active Withdrawn - After Issue
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101704513B (en) | Shunting-type isothermal sulfur-tolerant conversion process and equipment thereof | |
| CN103908929B (en) | A kind of methanol-to-olefins fixed bed production equipment combining heat exchange type muitishell and production method thereof | |
| CN202214306U (en) | Process device for preparing ethanol by utilizing acetic acid | |
| CN105642197A (en) | Large-sized reactor, and device and process thereof | |
| CN109748791B (en) | Energy-saving method for producing dimethyl adipate | |
| CN104826557A (en) | Synthesis reactor using self reaction heat to heat feed medium | |
| CN102274707A (en) | Slurry reactor used for producing liquid fuel | |
| CN102337159B (en) | Saturated hot water tower high-water-steam-ratio CO transformation process | |
| CN204134611U (en) | A kind of catalyst cleaning cooler | |
| CN103044187A (en) | Method and system for producing ethyl chloride | |
| CN204638162U (en) | A kind of ethanol is around pipe synthesis reactor | |
| CN202962427U (en) | Ethylene glycol hydrogenation reactor | |
| CN205235934U (en) | Adiabatic ethanol synthesis reactor | |
| CN204469677U (en) | A kind of adopting heat pipes for heat transfer radial bed methanator | |
| CN201933069U (en) | Decompression type biodiesel preparing device | |
| CN201358217Y (en) | Reactor for producing dimethyl ether from methanol through vapor-phase dehydration under pressurization | |
| CN203648501U (en) | Corrugated plate type uniform-temperature hydrogenation reactor | |
| CN101851152A (en) | Method for preparing dimethyl ether by methyl alcohol gaseous phase dehydration | |
| CN206308285U (en) | Synthesis reactor waste-heat methanol device in chloromethanes synthesis procedure | |
| CN202715401U (en) | Fixed bed catalytic reaction device capable of adjusting temperature of material at inlet | |
| CN206543591U (en) | A kind of polyester process tower | |
| CN102744018B (en) | Fixed bed catalytic reaction device with adjustable inlet material temperature | |
| CN201439492U (en) | Shunting isothermal sulphur-resisting conversion device | |
| CN2921008Y (en) | Separating heat tube type dimethyl ether reactor | |
| CN201880521U (en) | Device for continuously preparing medium-high carbon fatty acid ester |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20150916 Effective date of abandoning: 20151118 |
|
| C20 | Patent right or utility model deemed to be abandoned or is abandoned |