CN203750514U - Reactor for producing gasoline by using synthesis gas - Google Patents
Reactor for producing gasoline by using synthesis gas Download PDFInfo
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- CN203750514U CN203750514U CN201420100659.XU CN201420100659U CN203750514U CN 203750514 U CN203750514 U CN 203750514U CN 201420100659 U CN201420100659 U CN 201420100659U CN 203750514 U CN203750514 U CN 203750514U
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- beds
- tank body
- synthesis gas
- catalyst bed
- reactor
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model discloses a reactor for producing gasoline by using synthesis gas. The reactor comprises a tank body (2), an upper inlet (1), a lower outlet (9) and heating furnaces (4), wherein the upper inlet (1) is formed at the top part of the tank body (2); the lower outlet (9) is formed at the bottom part of the tank body (2); the tank body (2) is internally provided with three catalyst trays (7) which are arranged at the upper part, the middle part and the lower part; three catalyst bed layers, i.e., an upper catalyst bed layer (3), a middle catalyst bed layer (10) and a lower catalyst bed layer (8), are formed on the catalyst trays (7); gaps exist among the catalyst bed layers; each catalyst bed layer is provided with an independent heating furnace (4) and is internally provided with a thermocouple (6); a cooler (5) is arranged above the upper catalyst bed layer, the middle catalyst bed layer and the lower catalyst bed layer. The reactor disclosed by the utility model has the advantages that the structure is simple, and the purpose of organically combining methyl alcohol, dimethyl ether and gasoline in one reactor for reaction is achieved.
Description
Technical field
The utility model relates to a kind of chemosynthesis reaction device, is specially a kind of synthesis gas gasoline reactor processed.
Background technology
The few oil of the rich coal of China, contradiction between oil supply and demand is very outstanding.2.07 hundred million tons of Crude Oil in China output in 2012, crude oil consumption amount reaches 4.93 hundred million tons, and externally interdependency is 56.42%, is historical high.Expect the year two thousand twenty, the external interdependency of China's oil likely approaches 65%, and the Oil Safety of whole country, economic security, national security all can face very large challenge.Coal in China is but relatively abundant, coal gas is turned to synthesis gas and makes the technology of gasoline, has the strategic importance that ensures national energy security.
Synthesis gas gasoline processed comprises three steps: synthesising gas systeming carbinol, preparing dimethyl ether from methanol, dimethyl ether gasoline processed, and its reaction is as follows:
CO+2H
2→CH
3OH+102.5kJ (1)
CH
3OH→1/2(CH
3)
2O+1/2H
2O+10.1kJ (2)
1/2(CH
3)
2O→‐CH
2‐+1/2H
2O+34.7kJ (3)
This three step is all strong exothermal reactions.Wherein the reaction temperature of synthesising gas systeming carbinol is at 220～280 DEG C, preparing dimethyl ether from methanol reaction temperature is at 260～340 DEG C, dimethyl ether gasoline reaction temperature processed is at 340～420 DEG C, want to make three steps of synthesis gas gasoline processed to combine, must strictly control the reaction temperature of each section of reaction, make it not make reaction temperature raise because itself reacts liberated heat and produce temperature runaway phenomenon, cause the generation of side reaction and the inactivation of sintering of catalyst.Existing fixed bed reactors mostly are single beds, can not meet the requirement that three-step reaction carries out simultaneously.In utility model patent CN201068444Y, introduce a kind of preparing gasoline by methanol reactor, this reactor is provided with at least two catalytic bed in tank body, and between catalytic bed, be provided with cooler, what but all beds carried out is all preparing gasoline by methanol reactions, can not realize multistage independence temperature control, can not meet synthesis gas gasoline three-step reaction processed and organically be combined in a requirement in fixed bed reactors, therefore, invent and a kind ofly three-step reaction in gasoline processed synthesis gas is organically combined in to the fixed bed that completes integrated reacting in a fixed bed needs solution badly, do not find report through retrieval.
Summary of the invention
The purpose of this utility model is to provide a kind of simple in structure, realizes the synthesis gas gasoline reactor processed that methyl alcohol is synthetic, dimethyl ether is synthetic and the synthetic combination of gasoline is reacted at a reactor.
The utility model is realized by following technical scheme, it comprises tank body, upper inlet, lower outlet, heating furnace, it is characterized in that upper inlet is arranged at tank body top, tank base has lower outlet, in tank body, be provided with three of upper, middle and lower catalyst pallet, on catalyst pallet, form three of upper, middle and lower beds, have spacing between beds, each beds is provided with independently heating furnace, thermocouple in each beds has cooler on the beds of three of upper, middle and lower.
Heating furnace as above can be programme-control heating furnace.
Cooler as above is annular porous cold shock gas distributor.
Catalyst pallet as above is pottery or quartzy.
Because the life-span of dimethyl ether gasoline catalyzing agent processed is far smaller than the life-span of synthesising gas systeming carbinol and preparing dimethyl ether from methanol catalyst, so the life-span of shorter catalyst of life-span is reference in synthesising gas systeming carbinol and preparing dimethyl ether from methanol catalyst, dimethyl ether for subsequent use gasoline reactor processed, the life-span of coupling integer catalyzer, meet the long playing needs of W-response, facilitate the regeneration of catalyst, on lower beds, be also provided with dimethyl ether and export in order to connect dimethyl ether for subsequent use gasoline reactor processed.
In use and the course of work, first synthesising gas systeming carbinol catalyst is added upper beds, preparing dimethyl ether from methanol catalyst to add middle beds, dimethyl ether gasoline catalyzing agent processed to add lower beds, pressurization synthesis gas enters the upper inlet of synthesis gas gasoline reactor processed, then from top to bottom successively through catalytic bed, each beds is heated to corresponding reaction temperature by programme-control heating furnace independently.While passing each catalytic bed, there is respective reaction in each gas, produce a large amount of heats simultaneously, the amount that thermocouple can enter reactor according to the real time temperature control refrigerating gas of beds, refrigerating gas is synthesis gas or the reacted tail gas of not complete reaction, cold gas participates in reaction and circulation, and the heat in reactor is taken away.So just can reach the each reaction bed temperature of strict control and maintain in certain temperature range, greatly reduce energy consumption, save investment.
Compared with prior art, synthesis gas described in the utility model gasoline reactor processed organically by synthetic methyl alcohol, dimethyl ether is synthetic, gasoline synthetic three independently technical process combine, simplify significantly technical process, and take full advantage of the energy between each reaction, as the liquefaction of methanol steam and re-vaporization process are all omitted, the utilization rate that has greatly improved energy, has reduced energy consumption.The utility model can make synthesis gas directly react and generate gasoline, LPG and fuel gas therein, and ensures that easily each reaction bed temperature is controlled in target temperature range.
Brief description of the drawings
Fig. 1 is structural representation of the present utility model
As shown in the figure, 1 is upper inlet; 2 is tank body; 3 is upper beds; 4 is heating furnace; 5 is cooler; 6 is thermocouple; 7 is catalyst pallet; 8 is lower beds; 9 is lower outlet; 10 is middle beds; 11 is refrigerating gas; 12 is dimethyl ether outlet.
Detailed description of the invention
Embodiment 1
A kind of synthesis gas gasoline reactor processed, it comprises tank body 2, upper inlet 1, lower outlet 9, heating furnace 4, upper inlet 1 is arranged at tank body 2 tops, lower outlet 9 is arranged at tank body 2 bottoms, in tank body 2, be provided with, in, lower three catalyst quartz pallet 7, beds 3 on forming on catalyst pallet 7, middle beds 10 and 8 three beds of lower beds, between beds, there is spacing, each beds is provided with independently programme-control heating furnace 4, thermocouple 6 in each beds, upper, in, on lower three beds, there is annular porous cold shock gas profile cooler 5.
In use and the course of work, first synthesising gas systeming carbinol catalyst is added upper beds 3, preparing dimethyl ether from methanol catalyst to add middle beds 10, dimethyl ether gasoline catalyzing agent processed to add lower beds 8, pressurization synthesis gas enters upper inlet 1, then from top to bottom successively through catalytic bed 3,10,8, each beds is heated to corresponding reaction temperature by programme-control heating furnace 4 independently.While passing catalytic bed, there is respective reaction in each gas, produce a large amount of heats simultaneously, the amount that thermocouple 6 can regulate refrigerating gas 11 to enter reactor by annular porous cold shock gas profile cooler 5 according to the real time temperature of beds, make beds arrival end temperature maintain 230-250 DEG C, the port of export maintains 260-280 DEG C, middle beds arrival end temperature maintains 260-280 DEG C, the port of export maintains 320-350 DEG C, lower beds arrival end temperature maintains 320-350 DEG C, the port of export maintains 400-410 DEG C, refrigerating gas 11 is mist or the reacted tail gas of not complete reaction, refrigerating gas 11 participates in reaction and circulation, and the heat in reactor is taken away, reacted gasoline and hydrocarbon mixture are discharged from lower outlet 9.
Embodiment 2
Because the life-span of dimethyl ether gasoline catalyzing agent processed is far smaller than the life-span of synthesising gas systeming carbinol and preparing dimethyl ether from methanol catalyst, so taking life-span of shorter catalyst of life-span in synthesising gas systeming carbinol and preparing dimethyl ether from methanol catalyst as reference, on lower beds, be also provided with dimethyl ether outlet 12 in order to connect dimethyl ether for subsequent use gasoline reactor processed, the life-span of coupling integer catalyzer, meet the long playing needs of W-response, facilitate the regeneration of catalyst, all the other are with embodiment 1.
Claims (5)
1. a synthesis gas gasoline reactor processed comprises tank body (2), upper inlet (1), lower outlet (9), heating furnace (4), it is characterized in that upper inlet (1) is arranged at tank body (2) top, lower outlet (9) is arranged at tank body (2) bottom, tank body is provided with in (2), in, lower three catalyst pallets (7), on catalyst pallet (7), form upper beds (3), (8) three beds of middle beds (10) and lower beds, between beds, there is spacing, each beds is provided with independently heating furnace (4), thermocouple in each beds (6), upper, in, on lower three beds, there is cooler (5).
2. a kind of synthesis gas as claimed in claim 1 gasoline reactor processed, is characterized in that described heating furnace (4) is programme-control heating furnace.
3. a kind of synthesis gas as claimed in claim 1 gasoline reactor processed, is characterized in that described cooler (5) is annular porous cold shock gas distributor.
4. a kind of synthesis gas as claimed in claim 1 gasoline reactor processed, is characterized in that described catalyst pallet (7) is for pottery or quartzy.
5. a kind of synthesis gas gasoline reactor processed as described in claim 1-4 any one, is characterized in that being provided with dimethyl ether outlet (12) on lower beds (8).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420100659.XU CN203750514U (en) | 2014-03-06 | 2014-03-06 | Reactor for producing gasoline by using synthesis gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420100659.XU CN203750514U (en) | 2014-03-06 | 2014-03-06 | Reactor for producing gasoline by using synthesis gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203750514U true CN203750514U (en) | 2014-08-06 |
Family
ID=51245826
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420100659.XU Expired - Fee Related CN203750514U (en) | 2014-03-06 | 2014-03-06 | Reactor for producing gasoline by using synthesis gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203750514U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103849421A (en) * | 2014-03-06 | 2014-06-11 | 山西潞安矿业(集团)有限责任公司 | Integral process and reactor for preparing petroleum by using synthetic gas |
| CN108786664A (en) * | 2018-05-21 | 2018-11-13 | 合肥嘉科工贸有限公司 | A kind of multistage thermostatic type cold shocking type methanol synthesis reactor |
-
2014
- 2014-03-06 CN CN201420100659.XU patent/CN203750514U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103849421A (en) * | 2014-03-06 | 2014-06-11 | 山西潞安矿业(集团)有限责任公司 | Integral process and reactor for preparing petroleum by using synthetic gas |
| CN108786664A (en) * | 2018-05-21 | 2018-11-13 | 合肥嘉科工贸有限公司 | A kind of multistage thermostatic type cold shocking type methanol synthesis reactor |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140806 Termination date: 20200306 |