CN109225072A - A kind of synthesis reaction system and synthetic reaction method - Google Patents
A kind of synthesis reaction system and synthetic reaction method Download PDFInfo
- Publication number
- CN109225072A CN109225072A CN201811076179.3A CN201811076179A CN109225072A CN 109225072 A CN109225072 A CN 109225072A CN 201811076179 A CN201811076179 A CN 201811076179A CN 109225072 A CN109225072 A CN 109225072A
- Authority
- CN
- China
- Prior art keywords
- cooling medium
- pipeline
- synthesis
- tube
- reaction
- 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.)
- Granted
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
- B01J8/0085—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction promoting uninterrupted fluid flow, e.g. by filtering out particles in front of the catalyst layer
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Fluid Mechanics (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The present invention discloses a kind of synthesis reaction system and synthetic reaction method, is related to chemical equipment technical field, for reduce synthesis reactor tube side and shell side pressure difference and design.The synthesis reaction system includes: synthesis reactor and balance pipeline, and synthesis reactor includes: shell；Setting is tube side inside the intracorporal reaction tube of shell, reaction tube, is shell side outside reaction tube, feedstock pipeline, feedstock pipeline is connected to tube side；Cooling medium pipeline, cooling medium pipeline are connected to shell side, and cooling medium pipeline includes coolant feed pipes line and cooling medium discharging pipeline；Balance pipeline is connected to feedstock pipeline and cooling medium discharging pipeline.Synthesis reaction system provided by the invention and synthetic reaction method are for reducing the tube side of synthesis reactor and the pressure difference of shell side, reduce the wall thickness of reaction tube, the heat exchanged thermoresistance for reducing catalyst bed and cooling medium, improves the catalytic efficiency of catalyst and the yield of product.
Description
Technical field
The present invention relates to chemical equipment technical field more particularly to a kind of synthesis reaction system and synthetic reaction methods.
Background technique
Traditional alcohol synthesis reaction device has synthetic reaction and removes two effects of reaction heat, and common alcohol synthesis reaction device is
Vertical tube-type reactor, wherein loading catalyst inside tubulation, (tube side refers to flow of feed gas through in tubulation to unstripped gas in tube side
Channel) interior catalyst catalytic action under carry out alcohol synthesis reaction, while releasing heat, (shell side refers to cold shell side outside tubulation
But water flows through the channel outside tubulation) the cooling tubulation of cooling water is passed through to maintain temperature needed for alcohol synthesis reaction inside tubulation.
When alcohol synthesis reaction device is using cooling water heat exchange cooling, the inside and outside pressure difference of reactor tubulation is bigger, leads to
Often between 1-27Mpa, while the operating temperature of alcohol synthesis reaction device is up to 300-500 DEG C, so in the work of the high temperature and pressure
It is very high to the intensity requirement of alcohol synthesis reaction device when making condition progress alcohol synthesis reaction, cause alcohol synthesis reaction device tubulation tube wall
Thickness is big or tubulation internal diameter is small, and tubulation wall thickness is positively correlated with the thermal resistance of catalyst bed and cooling water heat exchange, and tubulation wall thickness is bigger
Then thermal resistance is bigger, if thermal resistance is unfavorable for controlling alcohol synthesis reaction device tubulation internal accelerator bed temperature greatly, influences unstripped gas and urges
It is combined to the yield and yield of alcohol；The small difficulty of processing for increasing alcohol synthesis reaction device of tubulation internal diameter, since difficulty of processing limits
Alcohol synthesis reaction device tubulation internal diameter processed cannot be too small, generally 15-40mm, leads to alcohol synthesis reaction device tubulation internal accelerator bed
Layer center and catalyst bed surface temperature difference are big, are further unfavorable for controlling alcohol synthesis reaction device tubulation internal accelerator bed
Temperature influences the yield and yield of feed gas catalytic synthol.
Summary of the invention
It is to pass through balance pipe that the embodiment of the present invention, which provides a kind of synthesis reaction system and synthetic reaction method, main purpose,
Line reduces the tube side of synthesis reactor and the pressure difference of shell side, to reduce the wall thickness of reaction tube, and then reduce catalyst bed with
The heat exchanged thermoresistance of cooling medium improves the catalytic efficiency of catalyst and the yield of product.
In order to achieve the above objectives, the embodiment of the present invention adopts the following technical scheme that
A kind of synthesis reaction system, comprising:
Synthesis reactor and balance pipeline；The synthesis reactor includes:
Shell；Reaction tube, the reaction tube are arranged in the shell, are tube side, the reaction inside the reaction tube
It is shell side outside pipe；Feedstock pipeline, the feedstock pipeline are connected to the tube side；Cooling medium pipeline, it is described cold
But medium pipeline is connected to the shell side, and the cooling medium pipeline includes coolant feed pipes line and cooling medium discharge nozzle
Line；Wherein, the balance pipeline is connected to the feedstock pipeline and cooling medium discharging pipeline, by the tube side
It is connected to the shell side.
Synthesis reaction system provided in an embodiment of the present invention is connected the tube side of synthesis reactor and shell side using balance pipeline
Lead to, so that the pressure in the pressure and shell side in tube side is equal or close, reduces the pressure that synthetic reactor for reacting pipe is born
Power, and then the wall thickness design of reaction tube can be reduced, reduce the heat exchanged thermoresistance of catalyst bed and cooling medium, it thus can be just
In control catalyst bed temperature, as far as possible ensure reaction bed temperature uniformity, improve catalyst catalytic efficiency and
The reaction efficiency of raw material, the final yield for improving product.
Optionally, the pipe thickness of the reaction tube is 0.02~1mm.
Optionally, the cross section transverse of the reaction tube is round or polygonized structure.
Optionally, the synthesis reaction system further include: heat exchanger, the heat exchanger have cooling medium entrance and cooling
Media outlet, the coolant feed pipes line are connected to the cooling medium outlet and the synthesis reactor of the heat exchanger
Cooling medium entrance, the cooling medium discharging pipeline are connected to the cooling medium outlet and the heat exchange of the synthesis reactor
The cooling medium entrance of device.
Optionally, the synthesis reaction system further include: surge tank, the surge tank have feed inlet, discharge port peace
Heng Kou, the cooling medium outlet of the feed inlet and the synthesis reactor, the discharge port are cold with the heat exchanger
But medium inlet is connected to, and the balance port is connected to the feedstock pipeline by the balance pipeline.
Optionally, the synthesis reaction system further include: knockout drum, the knockout drum have balance ports,
Charging port and discharge end, the balance ports are connected to the feedstock pipeline by the balance pipeline, it is described into
Expect the cooling medium outlet of port and the synthesis reactor, the discharge end and the cooling of the synthesis reactor are situated between
The connection of matter entrance.
Further, the knockout drum further include: replenishing port, the replenishing port are configured to the gas-liquid point
From supplementing cooling medium in tank.
Optionally, liquid seal structure is provided on the balance pipeline.
Another aspect of the present invention additionally provides a kind of synthetic reaction method using synthesis reaction system described above, packet
It includes:
The catalyst filling in tube side；
Unstripped gas is imported in the tube side with catalyst and carries out synthetic reaction, and cooling medium is imported in shell side,
To absorb the heat of synthetic reaction generation, and make the pressure difference of the tube side and the shell side default by the balance pipeline
Within the scope of.
Synthetic reaction method provided in an embodiment of the present invention, the synthetic reaction method are carrying out feed gas catalytic synthetic reaction
When, make the pressure difference in pressure and shell side in the tube side within preset range by balancing pipeline, i.e., it is equal or close,
Tube side and the poor larger phenomenon of shell side pressure are prevented, reduces catalyst bed and external thermal resistance, so that catalyst bed is released
The timely cooled medium of the heat put absorbs, and effectively controls the temperature of catalyst bed, improve unstripped gas catalyzes and synthesizes rate
With the production rate of product.
Optionally, boiling point of the cooling medium under synthetic reaction pressure is greater than or equal to synthesis reaction temperature.
Optionally, the cooling medium includes: coolant and/or cooling water, wherein the coolant is in synthetic reaction pressure
Boiling point under power is higher than synthesis reaction temperature.
Optionally, keep the pressure of the tube side and the shell side equal by the balance pipeline, or, the preset range
For 0KPa~5KPa.
Detailed description of the invention
Fig. 1 is a kind of structural schematic diagram of synthesis reaction system provided in an embodiment of the present invention；
Fig. 2 is the structural schematic diagram of another synthesis reaction system provided in an embodiment of the present invention；
Fig. 3 is a kind of structural schematic diagram of synthesis reactor provided in an embodiment of the present invention；
Fig. 4 is a kind of structural schematic diagram of the cross section of reaction tube provided in an embodiment of the present invention；
Fig. 5 is the structural schematic diagram of the cross section of another reaction tube provided in an embodiment of the present invention；
Fig. 6 is a kind of flow diagram of synthetic reaction method provided in an embodiment of the present invention.
Specific embodiment
Synthesis reaction system of the embodiment of the present invention and synthetic reaction method are described in detail with reference to the accompanying drawing.
In the description of the present invention, term " first ", " second " are used for description purposes only, and should not be understood as instruction or dark
Show relative importance or implicitly indicates the quantity of indicated technical characteristic.The feature of " first ", " second " is defined as a result,
It can explicitly or implicitly include one or more of the features.In the description of the present invention, unless otherwise indicated, " more
It is a " it is meant that two or more.
In the description of the present invention, it should be noted that unless otherwise clearly defined and limited, term " installation ", " phase
Even ", " connection " shall be understood in a broad sense, for example, it may be being fixedly connected, may be a detachable connection, or be integrally connected；It can
To be mechanical connection, it is also possible to be electrically connected；It can be directly connected, can also can be indirectly connected through an intermediary
The connection of two element inner segments.For the ordinary skill in the art, above-mentioned term can be understood at this with concrete condition
Concrete meaning in invention.
The terms "and/or", only a kind of incidence relation for describing affiliated partner, indicates that there may be three kinds of passes
System, for example, A and/or B, can indicate: individualism A exists simultaneously A and B, these three situations of individualism B.In addition, herein
Middle character "/" typicallys represent the relationship that forward-backward correlation object is a kind of "or".
On the one hand the embodiment of the present invention provides a kind of synthesis reaction system, referring to Figures 1 and 2, the synthetic reaction system
System includes synthesis reactor 1 and balance pipeline 4, and the synthesis reactor 1 has tube side 101 and shell side 102, the balance pipeline
4 are connected to the tube side 101 and the shell side 102.
In the art, referring to Fig. 3, the synthesis reactor 1 includes shell 1-1；Reaction tube 1-7；First tube sheet 1-6 and
Second tube sheet 1-8, wherein the reaction tube 1-7 is arranged in the shell 1-1, is the tube side inside the reaction tube 1-7
It is the shell side 102 outside 101, the reaction tube 1-7；The first tube sheet 1-6 and the second tube sheet 1-8 is arranged in the reaction
It the both ends pipe 1-7 and is connected to the reaction tube 1-7, and becomes reaction zone between the first tube sheet 1-6 and the second tube sheet 1-8.
For example, catalyst is packed in the tube side 101 and forms catalyst bed, raw material when carrying out alcohol synthesis reaction
Gas (mainly including carbon monoxide and hydrogen) enters in tube side 101, when carrying out alcohol synthesis under the catalytic action of catalyst, reaction
Temperature is 150 DEG C -450 DEG C, reaction pressure 1MPa-25MPa, i.e., the alcohol synthesis reaction is high-temperature high-voltage reaction, and due to this
Synthetic reaction is exothermic reaction, then can discharge more heat in tube side 101, by shell side 102 import cooling medium with
Absorb the heat in tube side 101.Tube side 101 is connected to the shell side 102 using balance pipeline 4, so that it may make tube side 101 and shell
Pressure in journey 102 is equal or close, is not in the larger phenomenon of pressure difference, thus can be reduced reaction tube 1-7 tube wall institute
The pressure of receiving can reduce the thickness of tube wall when designing reaction tube 1-7 if the pressure that reaction tube 1-7 tube wall is born is reduced
Degree, pipe thickness are reduced, and will reduce the heat exchange resistance of catalyst bed and cooling medium accordingly, synthetic reaction is discharged
Heat can in time cooled medium take away, with guarantee catalyst bed temperature be suitable for catalyst give full play to catalysis make
With finally effectively improving the combined coefficient of unstripped gas and the yield of alcohol.
It is due to being not necessarily to that the pipe thickness design of reaction tube 1-7 is thicker, the transverse shape of reaction tube 1-7 is not done in this way
It limits, it is exemplary referring to Fig. 4 and Fig. 5, it can be circle；It is exemplary again, be also possible to polygon, for example, rectangle, it is trapezoidal or
Person's hexagon；The transverse shape of reaction tube 1-7 can be symmetrical structure, be also possible to dissymmetrical structure, as shown in figure 5, institute
The transverse shape for stating reaction tube 1-7 is trapezium structure, and the altitude range of trapezoid cross section is 1~10mm, the length of trapezoid cross section
Degree is far longer than height, and the reaction tube 1-7 described so just becomes laminated structure, and the reaction tube 1-7 of structure can be further in the form of sheets
Reduce the inside and outside temperature difference of catalyst bed, guarantees that the operating temperature of catalyst bed is uniform, so that catalyst is urged
Change efficiency and reaches best.
In some embodiments, the pipe thickness of the reaction tube 1-7 is 0.02~1mm.Exemplary again, pipe thickness is
0.1~1mm；Exemplary again, pipe thickness is 0.1~0.5mm.Reaction tube in this way compared to existing 5~20mm significantly reduces
Pipe wall thickness.
Referring to Fig. 3, material inlet 1-5, coolant feed pipe inlet are offered on the shell 1-1 of the synthesis reactor 1
1-3, cooling medium discharge port 1-2 and outlet for product 1-9, wherein material inlet 1-5 and outlet for product 1-9 with pipe
Journey 101 is connected to, and the coolant feed pipe inlet 1-3 and cooling medium discharge port 1-2 are connected to shell side 102, and cooling medium goes out
Material mouth 1-2 close to the one end the material inlet 1-5, the coolant feed pipe inlet 1-3 close to the one end outlet for product 1-9,
Outlet for product 1-9 is located at the bottom end of shell 1-1, and material inlet 1-5 is located at the top of shell 1-1.
Exemplary, the bottom end the shell 1-1 is equipped with supporting leg 1-4, the quantity of the supporting leg 1-4 be it is multiple, to improve shell
The stability of body 1-1.
When specifically carrying out synthetic reaction, referring to Fig.1, feedstock pipeline 8 is connected to material inlet 1-5, and product goes out
Expects pipe line 5 is connected to outlet for product 1-9, coolant feed pipes line 13 and coolant feed pipe inlet in cooling medium pipeline
1-3 is connected to, and the cooling medium discharging pipeline 9 in cooling medium pipeline is connected to cooling medium discharge port 1-2.
In order to simplify the pipeline connection of equipment, referring to Fig.1, the balance pipeline 4 is connected to 8 He of feedstock pipeline
The cooling medium discharging pipeline 9, the tube side 101 is connected to the shell side 102.
After the cooling medium enters the absorption heat of shell side 102, shell side may be discharged with liquid phase, gas-liquid mixed or gas phase
102, if shell side 102 is discharged with liquid phase, boiling point of the cooling medium under synthetic reaction pressure is higher than synthesis reaction temperature,
For example, ethylene glycol, ionic liquid etc., and the cooling medium can be a kind of cooling medium, be also possible to a variety of cooling mediums
Mixing, still, boiling point of the mixed cooling medium under synthetic reaction pressure are higher than synthesis reaction temperature, in this way when the cooling
Medium enters in shell side 102 will not gasify after absorption heat, can directly be connected to balance pipeline 4 with feedstock pipeline 8, be
It prevents high-temperature liquid-phase cooling medium from entering in feedstock pipeline 8, liquid seal structure can be set on balance pipeline 4, such as Fig. 1 institute
Show, liquid seal structure can be U-bend structure, S-shaped bend pipe structure or other structures, without limitation to liquid seal structure at this.
In order to realize the recycling of liquid phase cooling medium, referring to Fig.1, the synthesis reaction system further include: heat exchanger
3, there is the heat exchanger 3 cooling medium entrance and cooling medium to export, and the coolant feed pipes line is connected to described change
The cooling medium entrance of the cooling medium outlet and the synthesis reactor 1 of hot device 3, the cooling medium discharging pipeline are connected to
The cooling medium entrance of the cooling medium outlet and the heat exchanger 3 of the synthesis reactor 1.Specifically, when high-temperature liquid-phase is cold
But after medium enters heat exchanger 3, by the coolant of heat exchanger 3 enter pipeline 6 importing coolant to High-temperature cooling medium into
High-temperature liquid-phase cooling medium is become low temperature liquid phase cooling medium by row heat exchange, is finally passed through low temperature liquid phase cooling medium cold
But medium feeding line is imported in synthesis reactor 1 and is reused again.The coolant discharge pipe line 7 of heat exchanger 3 is by heat exchange
Heat exchanger 3 is discharged in coolant afterwards.
Cooling medium is mixed into unstripped gas, the conjunction when reaction pressure of entire synthesis reaction system changes in order to prevent
At reaction system further include: surge tank 2, the surge tank 3 have feed inlet, discharge port and balance port, and the discharge port is located at
The bottom of the surge tank 2, the balance port are located at the top of the surge tank 2, and the feed inlet is located at the side of surge tank 2
Face, specifically, the feed inlet is connected to the outlet of the cooling medium of the synthesis reactor 1 by cooling medium discharging pipeline 9,
The discharge port is connected to the cooling medium entrance of the heat exchanger 3 by cooling medium surge tank pipeline 10, the balance port
The feedstock pipeline 8 is connected to by the balance pipeline 4.Make after High-temperature cooling medium enters surge tank 2 in gravity
It is collected at the lower part of surge tank 2 under, surge tank 2 is discharged by the discharge port.
Exemplary, in order to increase the pressure of the cooling medium entered in synthesis reactor 1, the synthesis reaction system is also wrapped
Include: circulating pump 12, the outlet of the circulating pump 12 are connected to the coolant feed pipes line 13, the entrance of the circulating pump 12
Pass through the cooling medium outlet into pump conduit 11 and the heat exchanger 3.
Exemplary, shell side 102 may be discharged with gas-liquid mixed in the cooling medium, if shell side is discharged with gas-liquid mixed
102, then the cooling medium includes one or more cooling mediums, boiling of part of cooling medium under synthetic reaction pressure
Point is higher than synthesis reaction temperature, for example, ethylene glycol, ionic liquid etc., boiling point of the part cooling medium under synthetic reaction pressure
Lower than synthesis reaction temperature, boiling point of the cooling medium mixed in this way under synthetic reaction pressure is equal to synthesis reaction temperature,
When specifically being cooled down, part cooling medium will gasify, and another part will exist with liquid phase, for example, ethylene glycol and water
The cooling medium mixed, after the cooling medium that ethylene glycol is mixed with water enters shell side 102, water therein is at least partly
Vapor can be flashed to, ethylene glycol will not evaporate, and shell side 102 finally is discharged with gas-liquid mixed.
In order to realize the recycling of liquid phase cooling medium, referring to Fig. 2, the synthesis reaction system further include: gas-liquid point
From tank 14, the knockout drum 14 has balance ports, charging port and discharge end, and the balance ports pass through described flat
Weighing apparatus pipeline 4 is connected to the feedstock pipeline, and such as Fig. 2 is described to balance the fluid-tight formed on pipeline 4 with U-bend structure
Structure, cooling medium outlet of the charging port by cooling medium discharging pipeline 9 and the synthesis reactor 1, institute
Discharge end is stated to be connected to by coolant feed pipes line 13 with the cooling medium entrance of the synthesis reactor 1.When gas-liquid is mixed
The High-temperature cooling medium of conjunction enters knockout drum 14 by cooling medium discharging pipeline 9 and carries out gas-liquid separation, isolated gas phase
It is discharged by byproduct steam pipeline 15, the liquid phase cooling medium after separation is again introduced into synthesis by coolant feed pipes line 13
Reactor 1 realizes the recycling of liquid phase cooling medium.
It is exemplary, the knockout drum 14 further include: replenishing port, the replenishing port are configured to the gas-liquid point
From cooling medium is supplemented in tank, for example, the supplement end can be passed through after isolated gas phase is discharged by byproduct steam pipeline 15
The cooling medium that mouth supplement is evaporated, exemplary, the replenishing port includes the first replenishing port and the second replenishing port, and
First replenishing port makes up line with first and 16 is connected to, and the second replenishing port makes up line with second and 17 is connected to, and can pass through first
The cooling medium that 16 supplements that make up line are evaporated, the cooling medium for making up line the other types of 17 supplements by second.
In some embodiments, gas also can be used as cooling medium to cool down shell side.
On the other hand the embodiment of the present invention additionally provides a kind of synthetic reaction method, and the synthetic reaction method is using above-mentioned
The synthesis reaction system carries out synthetic reaction, and referring to Fig. 6, the synthetic reaction method is specifically included:
S1: the catalyst filling in tube side 101.
S2: unstripped gas is imported in the tube side with catalyst and carries out synthetic reaction, and cooling medium is imported into shell side
It is interior, to absorb the heat of synthetic reaction generation, and so that the tube side and the pressure difference of the shell side is existed by the balance pipeline
Within preset range.
It is exemplary, the pressure of the tube side and the shell side can be made equal by the balance pipeline；It is exemplary again, pass through
The balance pipeline can make the pressure difference of the tube side and the shell side within 0KPa~5KPa preset range.Thus significantly
The pressure difference for reducing tube side and shell side reduces the pressure that catalyst bed outer wall is born, and then reduces catalysis in tube side
The heat exchanged thermoresistance of cooling medium in agent bed and shell side, meanwhile, the manufacture difficulty of processing of the synthesis reactor can be also reduced, so that
Sheet filling not only can also can be used in catalyst bed using tubular completion, can be further reduced catalyst by sheet filling
With the temperature difference on surface inside bed, the yield of product is finally improved.
When importing the cooling medium, boiling point of the cooling medium under synthetic reaction pressure is higher than synthetic reaction temperature
The low-temperature cooling media of degree, importing can be liquid phase, and the High-temperature cooling medium of discharge is also liquid phase, thus be can be used such as Fig. 1 institute
The synthesis reaction system stated carries out synthetic reaction；When boiling point of the cooling medium under synthetic reaction pressure is equal to synthetic reaction
When temperature, the low-temperature cooling media of importing can be liquid phase, and the High-temperature cooling medium of discharge is also gas-liquid mixed phase, can thus be adopted
Synthetic reaction is carried out with synthesis reaction system as described in Figure 2, for example, being mixed into cooling Jie using cooling water and coolant
Matter, and boiling point of the coolant under synthetic reaction pressure is higher than synthesis reaction temperature, mixes resulting cooling medium in this way and is closing
It just can be equal to synthesis reaction temperature at the boiling point under reaction pressure.Wherein, specific fluid moves towards above-mentioned and has been described in, this
Place repeats no more.
In the description of this specification, particular features, structures, materials, or characteristics can be real in any one or more
Applying can be combined in any suitable manner in example or example.
The above description is merely a specific embodiment, but scope of protection of the present invention is not limited thereto, any
Those familiar with the art in the technical scope disclosed by the present invention, can easily think of the change or the replacement, and should all contain
Lid is within protection scope of the present invention.Therefore, protection scope of the present invention should be based on the protection scope of the described claims.
Claims (12)
1. a kind of synthesis reaction system characterized by comprising synthesis reactor and balance pipeline；The synthesis reactor packet
It includes:
Shell；
Reaction tube, the reaction tube are arranged in the shell, are tube side inside the reaction tube, are shell outside the reaction tube
Journey；
Feedstock pipeline, the feedstock pipeline are connected to the tube side；
Cooling medium pipeline, the cooling medium pipeline are connected to the shell side, and the cooling medium pipeline includes cooling medium
Feeding line and cooling medium discharging pipeline；
Wherein, the balance pipeline is connected to the feedstock pipeline and cooling medium discharging pipeline, by the pipe
Journey is connected to the shell side.
2. synthesis reaction system according to claim 1, which is characterized in that the pipe thickness of the reaction tube be 0.02~
1mm。
3. synthesis reaction system according to claim 1, which is characterized in that the cross section transverse of the reaction tube be it is round or
Polygonized structure.
4. synthesis reaction system according to claim 1, which is characterized in that the synthesis reaction system further include:
There is cooling medium entrance and cooling medium to export for heat exchanger, the heat exchanger, the coolant feed pipes line connection
Cooling medium entrance in the cooling medium outlet and the synthesis reactor of the heat exchanger, the cooling medium discharging pipeline
It is connected to the cooling medium entrance of the cooling medium outlet and the heat exchanger of the synthesis reactor.
5. synthesis reaction system according to claim 4, which is characterized in that the synthesis reaction system further include:
Surge tank, the surge tank have feed inlet, discharge port and balance port, and the feed inlet is cold with the synthesis reactor
But media outlet is connected to, and the discharge port is connected to the cooling medium entrance of the heat exchanger, and the balance port passes through described flat
Weighing apparatus pipeline is connected to the feedstock pipeline.
6. synthesis reaction system according to claim 1, which is characterized in that the synthesis reaction system further include:
Knockout drum, the knockout drum have balance ports, charging port and discharge end, and the balance ports pass through
The balance pipeline is connected to the feeding line, and the cooling medium outlet of the charging port and the synthesis reactor connects
Logical, the discharge end is connected to the cooling medium entrance of the synthesis reactor.
7. synthesis reaction system according to claim 6, which is characterized in that the knockout drum further include: supplement end
Mouthful, the replenishing port is configured to supplement cooling medium into the knockout drum.
8. synthesis reaction system according to claim 1, which is characterized in that be provided with fluid-tight knot on the balance pipeline
Structure.
9. utilizing the synthetic reaction method of according to any one of claims 1 to 88 described in any item synthesis reaction systems, which is characterized in that described
Synthetic reaction method includes:
The catalyst filling in tube side；
Unstripped gas is imported in the tube side with catalyst and carry out synthetic reaction, and cooling medium is imported in shell side, to inhale
The heat that synthetic reaction generates is received, and makes the pressure difference of the tube side and the shell side in preset range by the balance pipeline
Within.
10. synthetic reaction method according to claim 9, which is characterized in that the cooling medium is in synthetic reaction pressure
Under boiling point be greater than or equal to synthesis reaction temperature.
11. synthetic reaction method according to claim 9, it is characterised in that: the cooling medium include: coolant and/
Or cooling water, wherein boiling point of the coolant under synthetic reaction pressure is higher than synthesis reaction temperature.
12. synthetic reaction method according to claim 9, it is characterised in that: make the tube side by the balance pipeline
It is equal with the pressure of the shell side, or, the preset range is 0KPa-5KPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811076179.3A CN109225072B (en) | 2018-09-14 | 2018-09-14 | Synthetic reaction system and synthetic reaction method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811076179.3A CN109225072B (en) | 2018-09-14 | 2018-09-14 | Synthetic reaction system and synthetic reaction method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109225072A true CN109225072A (en) | 2019-01-18 |
| CN109225072B CN109225072B (en) | 2021-04-16 |
Family
ID=65058399
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811076179.3A Active CN109225072B (en) | 2018-09-14 | 2018-09-14 | Synthetic reaction system and synthetic reaction method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109225072B (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2000170688A (en) * | 1998-12-04 | 2000-06-20 | Mitsubishi Heavy Ind Ltd | Axial flow fan |
| CN1785492A (en) * | 2005-11-09 | 2006-06-14 | 邰学林 | Isobaric internal cooling type high temperature high pressure chemical reactor |
| CN101221361A (en) * | 2008-01-18 | 2008-07-16 | 友达光电股份有限公司 | Pipeline pressure balancing system |
| CN101559342A (en) * | 2009-05-12 | 2009-10-21 | 石家庄正元塔器设备有限公司 | Gas-solid catalytic reaction heat exchange device and reaction heat exchange process |
| CN102121569A (en) * | 2010-12-21 | 2011-07-13 | 神华集团有限责任公司 | Liquid sealing device for centralized liquid drainage of gas conduit |
| CN102188936A (en) * | 2011-05-25 | 2011-09-21 | 太原理工大学 | Fixed bed reactor |
-
2018
- 2018-09-14 CN CN201811076179.3A patent/CN109225072B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2000170688A (en) * | 1998-12-04 | 2000-06-20 | Mitsubishi Heavy Ind Ltd | Axial flow fan |
| CN1785492A (en) * | 2005-11-09 | 2006-06-14 | 邰学林 | Isobaric internal cooling type high temperature high pressure chemical reactor |
| CN101221361A (en) * | 2008-01-18 | 2008-07-16 | 友达光电股份有限公司 | Pipeline pressure balancing system |
| CN101559342A (en) * | 2009-05-12 | 2009-10-21 | 石家庄正元塔器设备有限公司 | Gas-solid catalytic reaction heat exchange device and reaction heat exchange process |
| CN102121569A (en) * | 2010-12-21 | 2011-07-13 | 神华集团有限责任公司 | Liquid sealing device for centralized liquid drainage of gas conduit |
| CN102188936A (en) * | 2011-05-25 | 2011-09-21 | 太原理工大学 | Fixed bed reactor |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109225072B (en) | 2021-04-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2016119224A1 (en) | Isothermal and low temperature shift converter and shift conversion process thereof | |
| CN103240036A (en) | Temperature stress resistant heat transfer reactor and composite device and application thereof | |
| CN105833804B (en) | Steam ascending manner radial flow reactors | |
| CN201519571U (en) | Shell and tube reactor for producing chloroethylene by utilizing acetylene method | |
| CN104152157A (en) | Coke oven rising pipe heat exchanger | |
| AU2003230236B2 (en) | Reaction apparatus with a heat-exchanger | |
| CA2824448C (en) | Heat exchanger for the cooling of hot gases and heat exchange system | |
| JP2008208006A (en) | Regenerative heat-exchangeable decomposer to be used in hydrogen production apparatus | |
| CN109225072A (en) | A kind of synthesis reaction system and synthetic reaction method | |
| KR101923231B1 (en) | Exchanger-reactor for the production of hydrogen with an integrated steam generation bundle | |
| JP5312355B2 (en) | Reactor and reaction product manufacturing method using the same | |
| CN206793615U (en) | Tubular reaction system for gas-solid-liquid three-phase highly exothermic reaction | |
| CN207129957U (en) | A kind of hydrogen production units by carbinol using high-efficiency helical heat exchange of heat pipe | |
| CN202376982U (en) | Amidation reactor | |
| CN105413591A (en) | Multi-section type heat insulation fixed bed reactor for PX production | |
| CN216638914U (en) | Methanol hydrogen production converter and methanol hydrogen production device | |
| CN109012508B (en) | Fischer-Tropsch synthesis fixed bed reactor | |
| CN208599695U (en) | Horizontal shell and tube reactor | |
| CN202752008U (en) | Gas phase hydrogenation reactor | |
| CN114636091A (en) | Solid-state hydrogen storage tank of circulation type heat transfer | |
| KR20170129724A (en) | Boiling water reactor | |
| CN206444581U (en) | A kind of methyl alcohol synthetic reactor | |
| CN109046183A (en) | A kind of F- T synthesis fixed bed reactors thermal control system | |
| CN202420237U (en) | Coil pipe heater with double cavity bodies | |
| CN204122092U (en) | Thimble tube heat-exchanged reformer |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |