CN210252197U

CN210252197U - Axial wound tube synthesis reactor

Info

Publication number: CN210252197U
Application number: CN201920679995.7U
Authority: CN
Inventors: 王庆新; 王揽月; 李建新
Original assignee: Nanjing Dunxian Chemical Technology Co ltd
Current assignee: Nanjing Dunxian Chemical Technology Co ltd
Priority date: 2019-05-13
Filing date: 2019-05-13
Publication date: 2020-04-07
Anticipated expiration: 2029-05-13

Abstract

The utility model discloses an axial winding pipe synthesis reactor, which comprises an upper end enclosure, a lower end enclosure, a cylinder body, an upper ring pipe header, a lower ring pipe header, a catalyst frame body and a winding pipe; the upper end enclosure and the lower end enclosure are respectively arranged at the upper end and the lower end of the cylinder, the catalyst frame body is arranged in the cylinder, the winding pipe is arranged in the catalyst frame body along the axial direction of the cylinder, a gap between the winding pipe and the catalyst frame body is filled with a catalyst, and the upper ring pipe header and the lower ring pipe header are respectively communicated with the upper end and the lower end of the winding pipe. The utility model discloses simple structure, convenient to use will directly bury at a catalyst bed around the pipe heat exchange tube, and the heat conversion that directly emits the synthetic gas reaction shifts out the catalyst bed into steam, and the task of synthetic gas system natural gas just can be accomplished around a tub synthesis reactor to an axial, has that equipment is few, the flow is short, the investment is low, easy operation, the operation energy consumption is low, advantages such as heat recovery rate height.

Description

Axial wound tube synthesis reactor

Technical Field

The utility model relates to a chemical reaction device, in particular to an axial winding tube synthesis reactor.

Background

The prior art of preparing natural gas from synthesis gas adopts an adiabatic catalyst bed layer and a waste heat boiler technology, and H can be completed only by connecting three adiabatic bed layers and three waste heat boilers in series basically₂With CO or CO₂Generating a CH4 reaction synthesis task, and having the defects of more equipment, long flow, large investment, large heat loss and the like.

The tube-shell type reactor for carbonylation of ethylene glycol of synthetic gas, the carbonylation reactor at present adopts phi 32 x 2 heat exchange tube, the catalyst is filled in the tube, the heat is transferred by water outside the tube, the catalyst filling amount is small, it is difficult to meet the upsizing of the apparatus, a set of carbonylation reactor of 20 ten thousand tons of ethylene glycol/year apparatus needs at least 4 carbonylation reactors of DN4600 specification to run in parallel. The existing shell-and-tube reactor has large engineering investment and difficult field management, and has seriously influenced the large-scale development of the industry for preparing the glycol from the synthetic gas, while the scale of the domestic project for preparing the glycol from the synthetic gas which is under construction and reported is 40-180 ten thousand tons of glycol per year, and along with the continuous expansion of glycol capacity and the large-scale device, a novel large-scale glycol carbonylation and hydrogenation reactor is urgently needed to be developed.

SUMMERY OF THE UTILITY MODEL

The utility model discloses the technical problem that will solve lies in: how to simplify equipment and improve heat recovery rate, and provides an axial wound tube synthesis reactor.

The utility model solves the technical problems by the following technical proposal, and comprises an upper head, a lower head, a cylinder body, an upper ring canal header, a lower ring canal header, a catalyst frame body and a winding pipe; the upper end enclosure and the lower end enclosure are respectively arranged at the upper end and the lower end of the cylinder, the catalyst frame body is arranged in the cylinder, the winding pipe is arranged in the catalyst frame body along the axial direction of the cylinder, a gap between the winding pipe and the catalyst frame body is filled with a catalyst, and the upper ring pipe header and the lower ring pipe header are respectively communicated with the upper end and the lower end of the winding pipe.

As one of the preferred modes of the utility model, the upper cover passes through flange joint to the top of barrel, be provided with gas inlet on the upper cover and be used for the delivery port that the water route flows.

As one of the preferable modes of the present invention, the water outlet is provided with a water outlet pipe for connecting the upper ring pipe header.

As one of the preferred modes of the utility model, the bottom integrated into one piece of low head and barrel, be equipped with gas outlet on the low head and be used for the water inlet that the water route got into.

As one of the preferable modes of the utility model, be provided with the cap of giving vent to anger in the low head, the cap of giving vent to anger is located gas outlet.

In a preferred embodiment of the present invention, a support ring for supporting the catalyst frame is provided in the cylinder.

As one of the preferable modes of the present invention, the upper and lower ring pipe headers are annular and are respectively disposed at the upper and lower ends of the cylinder.

In a preferred embodiment of the present invention, a center support tube for supporting the catalyst frame is provided in the catalyst frame in the axial direction.

As one of the preferable modes of the utility model, the winding pipe is a multi-channel spiral pipe and is arranged upwards in a spiral way from the bottom of the barrel body to the top in sequence.

The included angle of each spiral pipe in the winding pipe is the same, the length is the same, and the number of the spiral pipes is gradually increased from inside to outside along the radial direction of the barrel body. Along with around the external diameter grow of pipe, arrange more spiral pipes, can ensure that whole heat transfer is even, the heat can be fast effectual conveying outside the reactor.

Compared with the prior art, the utility model has the following advantages: the utility model discloses simple structure, convenient to use, the utility model discloses axial winding pipe synthesis reactor is to adopting multistage adiabatic catalyst bed + waste heat boiler technique to current synthetic gas system natural gas, and equipment is many, the flow is long, the investment is big, a novel synthesis reactor that heat loss is big etc. defect development, directly bury the winding pipe heat exchange tube in a catalyst bed, directly turn into the steam that the synthetic gas reaction was given off and shift out the catalyst bed, and an axial winding pipe synthesis reactor just can accomplish the task of synthetic gas system natural gas, has advantages such as equipment is few, the flow is short, the investment is low, easy operation, the operation energy consumption is low, heat recovery rate is high;

the axial wound tube synthesis reactor of the utility model can also replace the existing shell-and-tube ethylene glycol carbonylation reactor, and compared with the existing shell-and-tube ethylene glycol carbonylation reactor with the same specification, the ethylene glycol productivity can be improved by more than 150%.

Drawings

Fig. 1 is a schematic structural diagram of the present invention.

Detailed Description

The embodiments of the present invention will be described in detail below, and the present embodiment is implemented on the premise of the technical solution of the present invention, and a detailed implementation manner and a specific operation process are given, but the scope of the present invention is not limited to the following embodiments.

Example 1

As shown in fig. 1, the present embodiment includes an upper head 3, a lower head 13, a cylinder 6, an upper loop header 4, a lower loop header 11, a catalyst frame 7, and a winding pipe 8; the upper end enclosure 3 and the lower end enclosure 13 are respectively arranged at the upper end and the lower end of the cylinder 6, the catalyst frame 7 is arranged inside the cylinder 6, the winding pipe 8 is axially arranged inside the catalyst frame 7 along the cylinder 6, a gap between the winding pipe 8 and the catalyst frame 7 is filled with a catalyst 10, and the upper ring pipe header 4 and the lower ring pipe header 11 are respectively communicated with the upper end and the lower end of the winding pipe 8.

The upper end enclosure 3 is connected to the top of the cylinder 6 through a flange 5, and a gas inlet 1 and a water outlet for water to flow out are arranged on the upper end enclosure 3.

And a water outlet pipe 2 used for connecting the upper ring pipe header 4 is arranged on the water outlet.

The bottom integrated into one piece of low head 13 and barrel 6, be equipped with gas outlet and the water inlet that is used for the water route to get into on the low head 13.

An air outlet cap 15 is arranged in the lower end enclosure 13, and the air outlet cap 15 is positioned on an air outlet.

A support ring 12 for supporting the catalyst frame 7 is provided in the cylinder 6.

The upper ring pipe header 4 and the lower ring pipe header 11 are annular and are respectively arranged at the upper end and the lower end of the cylinder 6.

A central support tube 9 for supporting the catalyst frame 7 is axially provided in the catalyst frame 7.

The winding pipe 8 is a plurality of spiral pipes with the same included angle and the same length, and the spiral pipes are sequentially upwards spirally arranged from the bottom to the top of the barrel 6.

The water inlet pipe 14, the lower ring pipe header, the winding pipe 8, the upper ring pipe header, the water outlet pipe 2 and other parts of the embodiment form a water flow path from bottom to top;

the gas inlet 1, the upper end enclosure 3, the catalyst frame body 7, the lower end enclosure 13, the gas outlet cap 15, the gas outlet pipe 16 and other components form a gas flow path from top to bottom;

the pressure-bearing container shell comprises a gas inlet 1, a water outlet, an upper seal head 3, a flange 5, a cylinder body 6, a support ring 12, a lower seal head 13, a water inlet pipe 14, an air outlet cap 15, an air outlet pipe 16 and the like.

The catalyst frame 7 of this example was filled with a Ni/Si catalyst to complete H₂With CO or CO₂Generating CH₄Reaction (3H)₂+CO→CH₄+H₂O+Q_Put、4H₂+CO₂→CH₄+2H₂O+Q_Put) And byproduct saturated steam of 4.0-10.0 MPa is produced, the temperature of the bed layer is controlled within the range of 260-550 ℃, and the three adiabatic catalyst bed layers and three waste heat boilers for preparing natural gas by using the existing synthetic gas can be replaced.

Example 2

In this example, the catalyst frame 7 was filled with Pd/AI₂O₃The carbonylation reaction catalyst of the system completes the carbonylation reaction of CO (CO + CH)₃ONO→(COOCH₃)₂+NO+Q_Put) And byproduct of 0.05-0.12 MPa saturated steam, and the temperature of the bed layer is controlled to beCompared with a shell-and-tube carbonylation reactor which operates in the same specification, the ethylene glycol productivity can be improved by more than 150 percent within the range of 108-145 ℃.

Other embodiments are the same as example 1.

The above description is only exemplary of the present invention and should not be taken as limiting the scope of the present invention, as any modifications, equivalents, improvements and the like made within the spirit and principles of the present invention are intended to be included within the scope of the present invention.

Claims

1. An axial winding synthesis reactor is characterized by comprising an upper end enclosure, a lower end enclosure, a cylinder, an upper ring pipe header, a lower ring pipe header, a catalyst frame body and a winding pipe; the upper end enclosure and the lower end enclosure are respectively arranged at the upper end and the lower end of the cylinder, the catalyst frame body is arranged in the cylinder, the winding pipe is arranged in the catalyst frame body along the axial direction of the cylinder, a gap between the winding pipe and the catalyst frame body is filled with a catalyst, and the upper ring pipe header and the lower ring pipe header are respectively communicated with the upper end and the lower end of the winding pipe.

2. The axial wound tube synthesis reactor according to claim 1, wherein the upper head is connected to the top of the barrel through a flange, and the upper head is provided with a gas inlet and a water outlet for water path outflow.

3. The axial wound tube synthesis reactor according to claim 2, wherein the water outlet is provided with a water outlet pipe for connecting with the upper loop header.

4. The axial wound tube synthesis reactor according to claim 1, wherein the lower head is integrally formed with the bottom of the barrel, and the lower head is provided with a gas outlet and a water inlet for water passage.

5. The axial wound tube synthesis reactor according to claim 4, wherein a gas outlet cap is arranged in the lower seal head, and the gas outlet cap is positioned on the gas outlet.

6. The axial wound tube synthesis reactor according to claim 1, wherein a support ring for supporting the catalyst frame is provided in the cylinder.

7. The axially wound tube synthesis reactor according to claim 1, wherein the upper and lower loop headers are annular and are disposed at the upper and lower ends of the cylindrical body, respectively.

8. The axial wound tube synthesis reactor according to claim 1, wherein a central support tube for supporting the catalyst frame is axially provided in the catalyst frame.

9. The axial wound tube synthesis reactor according to claim 1, wherein the wound tube is a plurality of spiral tubes which spiral upwards from the bottom to the top of the tube body in sequence.

10. The axial wound tube synthesis reactor according to claim 9, wherein each of the coils in the wound tube has the same included angle and the same length, and the number of the coils increases gradually from the inside to the outside along the radial direction of the tube body.