CN211754821U

CN211754821U - Self-heating type fixed bed reactor and system

Info

Publication number: CN211754821U
Application number: CN201921734699.9U
Authority: CN
Inventors: 袁清; 王少兵; 毛俊义; 黄涛
Original assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Current assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Priority date: 2019-10-16
Filing date: 2019-10-16
Publication date: 2020-10-27
Anticipated expiration: 2029-10-16

Abstract

A self-heating fixed bed reactor and a system thereof are composed of a reactor shell, a top feed inlet, a middle feed inlet, an inlet distribution device, a fluid collecting, mixing and distribution device, an outlet collector and an outlet; the reactor comprises a reactor shell, a top feed inlet, inlet distribution equipment, at least two catalyst beds, fluid collection, mixing and distribution equipment, a middle feed inlet, an outlet collector and a reactor bottom outlet, wherein the top feed inlet is arranged at the top of the reactor shell, the inlet distribution equipment is arranged at the top of the reactor shell and is communicated with the top feed inlet, at least two catalyst beds are arranged in the reactor shell, the fluid collection, mixing and distribution equipment is arranged between the two catalyst beds and is communicated with the middle feed inlet, and the outlet collector is arranged below the bottom catalyst bed in the reactor and is. The utility model provides a from getting hot type fixed bed reactor is applicable to the balanced or strong exothermic reaction system of solid phase catalysis heat release of liquid-liquid or gas-liquid feeding, get hot material and get the direct contact heat transfer in the reactor including one or stranded.

Description

Self-heating type fixed bed reactor and system

Technical Field

The present invention relates to a reactor apparatus in the field of petrochemical industry, and more particularly, to a fixed bed reactor for exothermic reaction processes.

Background

The fixed bed reactor is a reactor form filled with solid catalyst or solid reactant to realize heterogeneous reaction process, and has the advantages of simple structure, convenient operation, stable operation, small fluid back mixing, small mechanical loss of catalyst, etc. and is the most widely used reactor form in industry at present. The structure types of the fixed bed reactor are mainly divided into an adiabatic type and a heat exchange type, wherein the adiabatic type fixed bed is suitable for exothermic reaction with small reaction heat effect, the reaction process allows the reaction with wider variation range of temperature, the heat effect is larger, but the process is not very sensitive to the reaction temperature or the reaction rate is very fast; the heat exchange type fixed bed refers to a reaction device which takes away reaction heat by adopting a heat exchange medium.

In order to ensure the filling of the catalyst and the better distribution and flow of the fluid in the fixed bed reactor, a certain internal member needs to be installed inside the reactor, the commonly used internal members of the reactor mainly comprise various distributors, collectors, supporting structures and the like, and CN201020000158.6 discloses a liquid collecting, mixing and distributing device which is characterized in that a plurality of labyrinth members for enhancing the mixing of the fluid are arranged inside the liquid collecting, mixing and distributing device. CN100430458C discloses a fixed bed reactor, in which a mixing device with vertically placed vortex chambers is provided, and the main purpose is to mix the fluid and uniformly distribute the mixed fluid on the next bed.

For example, etherification generally refers to the reaction of methanol with tertiary olefins such as isobutylene and isoamylene to produce tertiary methyl alkyl ethers (MTBE, TAME, etc.), and is a typical exothermic reaction process controlled by thermodynamic equilibrium. The currently used forms of etherification reactors in industry mainly comprise fixed beds, expanded beds and catalytic distillation columns. The expanded bed etherification reactors disclosed in FR 2455019, FR 2440931 are effective in eliminating the hot spots of the reaction, but the backmixing of the material is severe, resulting in a reduction in the conversion. US4439350 discloses that a catalytic distillation technology is used for etherification to break the equilibrium limit and improve the reaction conversion rate, but the catalyst filling structure in the catalytic distillation tower is relatively complex and the application thereof is limited to a certain extent. The fixed bed reactor is widely used for etherification reaction because of its simple structure.

In order to solve the heat release problem in the chemical reaction process, a tubular reactor or a cylindrical reactor with reaction materials cooled in an external circulation mode is adopted in the traditional process. The tubular reactor has the advantages of complex equipment, large investment, high energy consumption and less application; and the reaction efficiency of the external circulation drum type reactor is reduced because the concentration of reactants is diluted by the circulating material flow. CN 200977456A discloses a bubble point reactor for preparing MTBE, the reaction is carried out in the range of the bubble point and dew point temperature of the materials, part of liquid components is changed into vapor phase after absorbing the reaction heat, and then the vapor phase flows out from a vapor phase pipeline arranged at the top of the reactor, thereby achieving the function of controlling the reaction temperature. However, this reactor is not suitable for feedstocks with too high an olefin content, since the heat of reaction vaporizes all of the methanol-C4 azeotrope and even the remaining C4, and the remaining heat also causes the bed temperature to continue to rise, leading to reverse decomposition of MTBE.

SUMMERY OF THE UTILITY MODEL

One of the technical problems to be solved in the utility model is to provide a fixed bed reactor of solid catalytic reaction system, which is liquid phase or gas-liquid phase and is used for the reaction process of strong heat release or thermodynamic equilibrium control.

The second technical problem to be solved by the present invention is to provide a fixed bed reaction system in the exothermic reaction process.

The utility model provides a self-heating fixed bed reactor, which consists of a reactor shell, a top feed inlet, a middle feed inlet, an inlet distribution device, a fluid collecting, mixing and distribution device, an outlet collector and an outlet; the reactor comprises a reactor shell, a top feed inlet, inlet distribution equipment, a fluid collection, mixing and distribution equipment, a middle feed inlet, an outlet collector and a gas-liquid separator, wherein the top feed inlet is arranged at the top of the reactor shell, the inlet distribution equipment is arranged at the top of the reactor shell and is communicated with the top feed inlet, at least two catalyst bed layers are arranged in the reactor shell, the fluid collection, mixing and distribution equipment is arranged between the two catalyst bed layers and is communicated with the middle feed inlet, and the outlet collector is arranged below the bottom catalyst bed layer in the reactor and.

The utility model provides a fixed bed reaction system adopts foretell self-heating formula fixed bed reactor, the reactor in fill multistage catalyst bed, load same kind or several kinds of solid acid catalyst in the different catalyst bed.

The utility model provides a from getting hot type fixed bed ware and reaction system's beneficial effect does:

the utility model provides an among the self-heating formula fixed bed ware, collect through top entry distributor and middle bed fluid and mix the dispensing equipment and can carry out high efficiency, collect fast and distribute reaction raw materials and middle fluid, effectively solved the longer problem of bed fluid maldistribution and intersegment fluid mixing degree in the multistage heat insulation fixed bed reactor among the prior art. The utility model provides a from getting hot type fixed bed reactor is in the use, adds through middle feed inlet and gets hot commodity circulation and can absorb the reaction heat, reduces bed temperature, is favorable to controlling the even running of reaction.

Drawings

Fig. 1 is a schematic structural view of a self-heating fixed bed reactor provided by the present invention;

FIG. 2 is a schematic view of an intermediate fluid collection, mixing and distribution apparatus;

FIG. 3 is a three-dimensional schematic view of a spiral baffle within the secondary mixing chamber.

Wherein:

1-top feed inlet, 2-middle feed inlet, 3-reactor shell, 4-inlet distributor, 5-inlet distribution plate, 6, 8-catalyst bed layer, 7-collecting mixing distributor, 9-outlet collector, 10-material outlet; 11-top support plate, 12-guide plate, 13-external fluid distribution pipe, 14-primary mixing chamber, 15-secondary mixing chamber, 16-distribution plate and 17-bottom support plate.

Detailed Description

The following describes the embodiments of the present invention in detail.

In the present specification, the "upper part" of the container means a position from the bottom to the top of 0 to 50% of the container, the "lower part" of the container means a position from the bottom to the top of 50 to 100% of the container, the "middle part" of the container means a position from the bottom to the top of 30 to 70% of the container, and the "bottom part" of the container means a position from the bottom to the top of 95 to 100% of the container.

The utility model provides an among the self-heating fixed bed reactor, entry distribution equipment constitute by entry distributor and entry plate of distributor.

The inlet distributor is used for buffering, guiding and pre-distributing material flow and is selected from a perforated plate type structure, a screen mesh structure, a side gap type structure or other improved structures.

The inlet distribution plate can adopt a conventional structure, and for single liquid phase or gas phase feeding, the inlet distribution plate is selected from conventional gas phase or liquid phase distributors, such as a branch pipe type, a ring pipe type and the like; for gas-liquid mixed feeding, the gas-liquid distribution disc can be selected from a tower disc type, a long and short tube type, a bubble cap type or other conventional gas-liquid distribution discs.

The fluid collecting, mixing and distributing device comprises a top support plate 11, a guide plate 12, an external fluid distribution pipe 13, a mixing chamber, a fluid distribution disc 16 and a bottom support plate 17 which are spaced from top to bottom, wherein the mixing chamber consists of an external annular primary mixing chamber 14 and a secondary mixing chamber 15 positioned in the center; the external fluid distribution pipe 13 is a circular or grid pipeline with small holes and is communicated with the middle feed inlet; the fluid distribution plate is provided with small holes.

Preferably, the guide plate 12 is a conical plate with a cone angle of 140 ° to 175 °. The fluid from the catalyst bed on the top support plate enters the preliminary mixing chamber 14 through the deflector plate and is preliminarily mixed with the external fluid from the external fluid distribution pipe in the preliminary mixing chamber.

Preferably, the secondary mixing chamber is surrounded by an inner layer and an outer layer of cylindrical barrels with openings, a guide plate at the top and a bottom plate with a circular opening at the bottom, and the diameter of the barrels in the secondary mixing chamber is 1/3-3/4 of the diameter of the outer barrels.

The two layers of cylindrical barrels inside and outside the secondary mixing chamber are provided with openings, and the shapes of the openings can be circular, triangular, trapezoidal or spiral. The outer layer cylindrical barrel open pores and the inner layer cylindrical barrel open pores are arranged in a staggered order on the circumference. Preferably, circular holes are formed in the two layers of cylindrical barrels, the diameter of the opening 6 of the outer barrel is 5-50mm, preferably 6-30mm, and the diameter of the opening 8 of the inner barrel is 3-40mm, preferably 5-25 mm.

Preferably, the external fluid distribution pipe 13 is a ring-shaped pipe with small holes, and the diameter of the ring is larger than that of the outer cylindrical barrel of the secondary mixing chamber.

Preferably, the pipe diameter of the external fluid distribution pipe is 20-200mm, more preferably 30-150mm, round holes with the diameter of 2-20mm are formed on the external fluid distribution pipe, and the distance between the round holes is 10-200mm, preferably 20-100 mm.

Preferably, staggered baffles are distributed in the secondary mixing chamber, and the baffles can be rectangular, spiral, folded rectangular and the like, or wire mesh and corrugated packing to enhance mixing strength. The material flow after the primary mixing in the primary mixing chamber enters the secondary mixing chamber for further mixing through the opening channel on the cylinder outside the secondary mixing chamber. The fully mixed fluid enters a fluid distribution plate at the lower part of the secondary mixing chamber through an opening on the bottom plate of the secondary mixing chamber and is uniformly distributed, and then enters a lower section catalyst bed layer.

The top support plate and the bottom support plate of the fluid collecting, mixing and distributing device are both covered by Johnson nets or metal wire nets to support the solid catalyst bed layer and prevent the catalyst from leaking.

The utility model provides a from getting hot type fixed bed reactor is applicable to the solid phase catalytic reaction system of liquid-liquid or gas-liquid feeding. The reaction system comprises reaction processes such as etherification, esterification, hydrolysis, alkylation and the like which are controlled by thermodynamic equilibrium and intensive thermal reaction processes such as oxidation, hydrogenation and the like, wherein a solid catalyst is adopted in the reaction, and the reaction material is fed into a liquid phase or a gas-liquid two phase. In the using process, a heat taking material flow is added from the middle feeding hole, and the heat taking material flow comprises reaction raw materials, one or more of the reaction raw materials, reactor outlet products, non-reaction components and any combination of the materials. The axial upward hot material flow of the reactor can be upward in and downward out, and also can be downward in and upward out.

The solid acid catalyst is selected from one or more of a catalyst containing a molecular sieve, a cation ion exchange resin catalyst, a heteropoly acid catalyst and a catalyst loaded with heteropoly acid.

The following describes the self-heating fixed bed reactor and the reaction system provided by the present invention with reference to the accompanying drawings, but the present invention is not limited thereto.

Fig. 1 is a schematic structural view of a self-heating fixed bed reactor provided by the present invention, as can be seen from fig. 1, the self-heating fixed bed reactor provided by the present invention is composed of a reactor shell 3, a top feed inlet 1, a middle feed inlet 2, an inlet distribution device, a fluid collecting, mixing and distribution device 7, an outlet collector 9 and a material flow outlet 10; the reactor comprises a reactor shell, a top feed inlet 1, an inlet distribution device, a middle feed inlet 2, a fluid collection, mixing and distribution device 7, a top feed inlet 1, an inlet distribution disc 5, an inlet distributor 4, a fluid collection, mixing and distribution device 6, 8, an outlet collector, a material flow outlet 10 and a reactor shell, wherein the top feed inlet 1 is arranged at the top of the reactor shell, the inlet distribution device consists of the inlet distributor 4 and the inlet distribution disc 5, the inlet distribution device is arranged inside the reactor and communicated with the top feed inlet 1, the reactor shell is internally provided with the at least two sections of catalyst bed.

Fig. 2 is a schematic structural diagram of an intermediate fluid collecting, mixing and distributing device, and as shown in fig. 2, the fluid collecting, mixing and distributing device 7 includes a top support plate 11, a guide plate 12, an external fluid distribution pipe 13, a mixing chamber, a fluid distribution plate 16 and a bottom support plate 17 which are spaced from top to bottom, wherein the mixing chamber is composed of an external annular primary mixing chamber 14 and a centrally located secondary mixing chamber 15; the external fluid distribution pipe 13 is a circular or grid pipeline with small holes and is communicated with the middle feed port 2; the fluid distribution plate 16 is perforated with small holes.

The utility model provides a from getting hot type fixed bed reactor in the use, reaction raw materials gets into from top feed inlet 1, gets into catalyst bed 6 and catalyst contact reaction and exothermic after entry distributor 4 and 5 evenly distributed of entry distributor disk. The intermediate feed is fed from the intermediate feed inlet 2 in the middle section of the reactor and enters the preliminary mixing chamber 14 through the external fluid distribution pipe 13. The material flow from the upper catalyst bed layer 6 is guided by the guide plate 12 and then enters the primary mixing chamber 14, and two different fluids are primarily mixed and subjected to heat exchange in the primary mixing chamber. The mixed fluid enters the secondary mixing chamber 15 through the opening in the baffle of the outer cylinder between the primary mixing chamber 14 and the secondary mixing chamber 15 for further mixing. The secondary mixing chamber 15 is distributed with staggered baffles or wire mesh and corrugated packing to obtain higher mixing effect. Wherein a three-dimensional schematic diagram of the spiral baffle in the secondary mixing chamber is shown in figure 3. Cold and hot fluids are fully contacted, mixed and heat-exchanged, then enter the fluid distribution disc 16 through an opening on the bottom plate of the secondary mixing chamber 15, are uniformly distributed by the fluid distribution disc 16, enter the next section of catalyst bed layer 8 for continuous reaction, and finally a reaction product 10 is collected by an outlet collector 9 at the bottom of the reactor and then is extracted from the reactor.

The following comparative examples and examples further illustrate the effect of the self-heating fixed bed reactor provided by the present invention.

Comparative example 1

The etherification reaction of the light gasoline and the methanol is carried out by adopting a traditional adiabatic fixed bed reactor, and the height-diameter ratio of the reactor is 20. The material flow goes in and out from the top, a side gap type inlet distributor is arranged at the inlet of the reactor, and the material flow in the reactor is naturally distributed. The composition of etherification raw materials is shown in Table 1, wherein the mass fraction of tertiary carbon olefin with etherification activity is 50.3 percent, the alcohol-olefin ratio is 1.05, and the space velocity is 2.0h^-1A resin catalyst (D005-II, Special resin of Dandong Mingzhu, Ltd.) was used. The inlet temperature of the reactor was 55 ℃ and the pressure was 0.6 MPa. The results of the etherification reaction are shown in Table 2.

Example 1

Embodiment 1 adopts the utility model provides a from getting hot type fixed bed reactor, the reactor structure is shown as attached figure 1, the same comparative example of reactor basic dimension, the catalyst bed divide into the three-section, and the centre is equipped with two fluid collection mixing apparatus, and its structure is shown as figure 2, and the guide plate cone angle is 160, and the indoor outer barrel diameter ratio of secondary mixing is 1/2, all is equipped with staggered arrangement's round hole, round hole diameter 10mm on the interior outer barrel. The baffle inside the secondary mixing chamber adopts a spiral baffle as shown in figure 3. The reactor inlet feed composition and catalyst were the same as the comparative examples, catalyst loading and total plant throughput were the same as the comparative examples, and other reaction conditions were the same as the comparative examples.

The catalyst is filled in three bed layers, comprises two middle feed inlets, takes the same heat medium as the inlet feed of the reactor, and enters the reactor in two paths. The flow ratio of the three feeding materials from top to bottom is 3:5: 2. The results of the etherification reaction are shown in Table 2.

Example 2

Example 2 the same reactor equipment as in example 1 was used, the reactor inlet feed composition and catalyst were the same as in the comparative example, the catalyst loading and fresh feed throughput were the same as in the comparative example, and other reaction conditions were the same as in the comparative example. The catalyst was packed in two beds with one intermediate feed port, the difference to example 1 being that the secondary mixing was internally packed with wire mesh packing. Taking a heat medium as a cooled reactor outlet product, wherein the mass ratio of the intermediate feeding amount to the inlet feeding amount is 1: 1. The results of the etherification reaction are shown in Table 2.

TABLE 1

TABLE 2

Claims

1. A self-heating fixed bed reactor is characterized by comprising a reactor shell, a top feeding hole, a middle feeding hole, inlet distribution equipment, fluid collecting, mixing and distribution equipment, an outlet collector and an outlet, wherein the top feeding hole is arranged on the reactor shell; the reactor comprises a reactor shell, a top feed inlet, inlet distribution equipment, at least two catalyst beds, fluid collection, mixing and distribution equipment, a middle feed inlet, an outlet collector and a reactor bottom outlet, wherein the top feed inlet is arranged at the top of the reactor shell, the inlet distribution equipment is arranged at the top of the reactor shell and is communicated with the top feed inlet, at least two catalyst beds are arranged in the reactor shell, the fluid collection, mixing and distribution equipment is arranged between the two catalyst beds and is communicated with the middle feed inlet, and the outlet collector is arranged below the bottom catalyst bed in the reactor and is.

2. A self-heating fixed bed reactor as recited in claim 1, wherein said inlet distribution means comprises an inlet distributor and an inlet distribution plate.

3. The self-heating fixed bed reactor in accordance with claim 1, wherein the fluid collecting, mixing and distributing device comprises a top support plate (11), a guide plate (12), an outer fluid distribution pipe (13), a mixing chamber, a fluid distribution plate (16) and a bottom support plate (17) which are spaced from top to bottom, wherein the mixing chamber is composed of an outer annular primary mixing chamber (14) and a centrally located secondary mixing chamber (15); the external fluid distribution pipe (13) is a circular or grid pipeline with small holes and is communicated with the middle feed inlet; the fluid distribution plate is provided with small holes.

4. A self-heating fixed bed reactor as defined in claim 3, wherein said deflector (12) is a conical plate having a cone angle of 140 ° to 175 °.

5. A self-heating fixed bed reactor as defined in claim 3, wherein said secondary mixing chamber (15) is surrounded by an inner and an outer cylindrical bodies with openings, a top deflector and a bottom plate with a circular opening at the bottom.

6. The self-heating fixed bed reactor as recited in claim 5, wherein the diameter of the inner cylindrical shell of said secondary mixing chamber is 1/3-3/4 of the diameter of the outer cylindrical shell.

7. The self-heating fixed bed reactor as recited in claim 5, wherein the cylindrical bodies of the inner and outer layers of the secondary mixing chamber are provided with openings, and the openings of the cylindrical bodies of the outer layer and the openings of the cylindrical bodies of the inner layer are arranged in a staggered order on the circumference.

8. The self-heating fixed bed reactor as recited in claim 7, wherein the inner and outer cylindrical bodies have circular holes, the diameter of the hole in the outer cylindrical body is 5-50mm, and the diameter of the hole in the inner cylindrical body is 3-40 mm.

9. The self-heating fixed bed reactor as recited in claim 8, wherein the diameter of the opening of said outer cylindrical shell is 6-30mm, and the diameter of the opening of said inner cylindrical shell is 5-25 mm.

10. A self-heating fixed bed reactor as recited in claim 3, wherein said external fluid distribution tube is a small perforated circular tube having a diameter greater than the diameter of the outer cylindrical shell of said secondary mixing chamber.

11. A self-heating fixed bed reactor as recited in claim 3, wherein said external fluid distribution pipe has a diameter of 20-200mm, and has round holes with a diameter of 2-20mm, and the distance between the holes is 10-200 mm.

12. The self-heating fixed bed reactor as recited in claim 3, wherein said secondary mixing chamber is internally distributed with staggered baffles in the shape of a rectangle, a spiral, a folded rectangle, or a wire mesh, corrugated packing.

13. A self-heating fixed bed reactor as recited in claim 3, wherein said top support plate and said bottom support plate are covered with a johnson mesh or wire mesh to support the solid catalyst bed and prevent catalyst loss.

14. A fixed bed reaction system, characterized in that, the self-heating fixed bed reactor as claimed in any one of claims 1 to 13 is used, the reactor is filled with a plurality of catalyst beds, and different catalyst beds are filled with one or more solid acid catalysts.

15. A fixed bed reaction system as claimed in claim 14 wherein said solid acid catalyst is selected from one or more of a molecular sieve containing catalyst, a cationic ion exchange resin catalyst, a heteropolyacid catalyst and a supported heteropolyacid catalyst.