Methanol reforming and catalytic heating integrated reactor

Abstract

The utility model relates to the technical field of methanol-water hydrogen production equipment, in particular to a methanol reforming and catalytic heating integrated reactor which comprises a reactor and a first shell arranged in the reactor, a reforming reaction layer used for reforming reaction is arranged in the first shell, and a catalytic heating layer is arranged in the first shell. And the reactor is provided with a methanol raw material liquid feeding pipe and a high-purity hydrogen outlet which are communicated with the reforming reaction layer. The preheating vaporizer, the methanol reforming reactor, the catalytic oxidation heat-conducting oil furnace and other devices are integrally formed and integrated in the same device, stable operation of the devices is achieved through logic control, and the catalytic oxidation layer and the reforming reaction layer are stacked, so that the catalytic oxidation layer and the reforming reaction layer are stacked, and the catalytic oxidation layer and the reforming reaction layer are stacked. According to the present invention, the annular reforming reactor and the catalytic reactor are combined so as to provide the heat provided by the catalytic reaction for the reforming reaction as far as possible, increase the contact area of the reaction, and improve the reaction efficiency;

Description

TECHNICAL FIELD

[0001] The utility model relates to methanol water hydrogen production equipment technical field especially relates to a kind of methanol reforming and catalytic heating integrated reactor. BACKGROUND

[0002] Traditional methanol hydrogen production process route is: methanol and desalted water are mixed according to certain proportion, enter gasification heat exchanger and are gasified and superheated to the required temperature, complete gas phase catalytic cracking and conversion 2 reactions under the action of catalyst, generate conversion gas containing CO2, H2, CO, conversion gas is cooled after heat exchanger and condenser, and unreacted methanol is purified and recovered, finally into pressure swing adsorber and obtains high-purity hydrogen.

[0003] The existing technical problem is: the reaction process of methanol reforming hydrogen production device needs preheating vaporizer, methanol reforming reactor, catalytic oxidation heat conducting oil furnace and other multiple equipment to start together, and the device is not good enough in centralization, causing reaction raw materials to stay in the device for too long, methanol hydrogen production reaction itself belongs to endothermic reaction, if stay for too long, it will lead to increased heat loss, reduce reaction efficiency, and easily produce side reaction. UTILITY MODEL CONTENT

[0004] Therefore, the utility model aims at providing a kind of methanol reforming and catalytic heating integrated reactor to solve the technical problems, such as low centralization of existing methanol water hydrogen production equipment, and then low reaction efficiency.

[0005] Based on the above purpose, the utility model provides a kind of methanol reforming and catalytic heating integrated reactor, comprising: reactor and first shell in the reactor, the first shell is equipped with the reforming reaction layer for reforming reaction, the reactor is provided with methanol raw material liquid feed pipe and high-purity hydrogen outlet that communicate reforming reaction layer, the methanol raw material liquid feed pipe is connected with preheating vaporizer, the reactor and first shell form catalytic oxidation layer for catalytic oxidation reaction between them, the reactor is provided with air inlet pipe and discharge pipe that communicate catalytic oxidation layer, the high-purity hydrogen outlet is provided with separator for separating hydrogen in reforming reaction product, the high-purity hydrogen outlet is provided with shunt hole for communicating catalytic oxidation layer.

[0006] As the preferred technical scheme of the utility model, a pair of baffle plates is vertically arranged in the first shell, a current collector cover is arranged between the baffle plates, the outer side of the current collector cover, the opposite side of the baffle plate and the inner side of the first shell jointly form a first catalyst layer, the opposite side of the baffle plate and the inner side of the current collector cover jointly form a reforming reaction layer, the baffle plate at the upper end is provided with a current collecting hole connected to the first catalyst layer, and the current collector cover is provided with a first through hole for connecting the reforming reaction layer and the first catalyst layer.

[0007] As the preferred technical scheme of the utility model, the lower end of the partition plate is provided with a cap, a center pipe is arranged through the inside of the first shell, the center pipe penetrates the first shell and the reactor and forms a high-purity hydrogen gas outlet at the bottom end.

[0008] As the preferred technical scheme of the utility model, the second shell is further arranged between the reactor and the first shell, a second catalyst layer is formed between the outside of the second shell and the inner wall of the reactor, a catalytic oxidation layer is formed between the inside of the second shell and the outside of the first shell, and a second through hole is formed in the surface of the second shell and connects the second catalyst layer and the catalytic oxidation layer.

[0009] As the preferred technical scheme of the utility model, the preheating vaporizer penetrates the second catalyst layer and the catalytic oxidation layer in sequence, so that the catalytic oxidation reaction in the catalytic oxidation layer can heat the preheating vaporizer.

[0010] As the preferred technical scheme of the utility model, the air inlet pipe is arranged obliquely above the reactor, and the air inlet pipe penetrates the reactor and connects the catalytic oxidation layer.

[0011] As the preferred technical scheme of the utility model, the unloading pipe is arranged obliquely below the second shell, and the unloading pipe penetrates the reactor.

[0012] As the preferred technical scheme of the utility model, the axial lines of the reactor, the first shell and the second shell coincide with each other.

[0013] As the preferred technical scheme of the utility model, the separator comprises a conversion gas cooling condenser, a gas-liquid separator, a conversion gas purifier and a pressure swing adsorption separator.

[0014] The utility model has the advantages that the preheating vaporizer, the methanol reforming reactor, the catalytic oxidation heat conducting oil furnace and other devices are integrally formed and integrated in the same device, and through logical control, the device is stably operated, the catalytic oxidation layer and the reforming reaction layer are superposed, the annular reforming reactor and the catalytic reactor are combined, the heat provided by the catalytic reaction is provided to the reforming reaction as much as possible, the contact area of the reaction is increased, and the reaction efficiency is improved. BRIEF DESCRIPTION OF DRAWINGS

[0015] In order to more clearly illustrate the technical scheme in the utility model or the prior art, the following will briefly introduce the drawings needed to be used in the embodiment or the prior art description, and obviously, the drawings in the following description are only the utility model, and other drawings can be obtained by those skilled in the art without creative labor.

[0016] Figure 1The utility model discloses a reactor half -sectional perspective structure schematic diagram;

[0017] Figure 2 The utility model discloses a reactor main view half -sectional structure schematic diagram;

[0018] Figure 3 The utility model discloses a top -down principle structure schematic diagram;

[0019] Figure 4 The utility model discloses a process flow schematic diagram.

[0020] Marked as: 1, reactor;2, methanol raw material liquid feed pipe;3, preheating vaporizer;4, first shell;5, partition;6, confluence hole;7, confluence cover;8, first through -hole;9, cap cover;10, center tube;11, separator;12, high -purity hydrogen gas export;13, shunt hole;14, second shell;15, second through -hole;16, air inlet pipe;17, unloading pipe. DETAILED DESCRIPTION

[0021] In order to make the utility model's purpose, technical scheme and advantage more clearly, the following is in combination with specific embodiment, and the utility model is further detailed.

[0022] It is to be noted that, unless otherwise defined, the technical terms or scientific terms used in the utility model should be understood as the usual meaning of the person skilled in the art to which the utility model belongs. The "first", "second" and similar words used in the utility model do not represent any order, quantity or importance, but only distinguish different components. "Include" or "contain" and similar words mean that the element or object before the word covers the element or object listed after the word and its equivalent, and does not exclude other elements or objects. "Connect" or "connected" and similar words are not limited to physical or mechanical connection, but can include electrical connection, whether direct or indirect. "Up", "down", "left", "right" and the like are only used to represent relative positional relationship, when the absolute position of the described object changes, the relative positional relationship can also change accordingly.

[0023] As Figure 1 , Figure 2 and Figure 3As shown, a methanol reforming and catalytic heating integrated reactor comprises a reactor 1 and a first shell 4 arranged in the reactor 1, the first shell 4 is provided with a reforming reaction layer for reforming reaction, the reactor 1 is provided with a methanol raw material liquid feeding pipe 2 communicating with the reforming reaction layer and a high-purity hydrogen outlet 12, the methanol raw material liquid feeding pipe 2 is connected with a preheating vaporizer 3, a catalytic oxidation layer for catalytic oxidation reaction is formed between the reactor 1 and the first shell 4, the reactor 1 is provided with an air inlet pipe 16 and a discharge pipe 17 communicating with the catalytic oxidation layer, the high-purity hydrogen outlet 12 is provided with a separator 11 for separating hydrogen in the reforming reaction product, and the high-purity hydrogen outlet 12 is provided with a shunt hole 13 for communicating with the catalytic oxidation layer; the separator 11 comprises a conversion gas cooling condenser, a gas-liquid separator, a conversion gas purifier and a pressure swing adsorption separator, and is used for separating H2, CO and CO2 mixed gas after reforming reaction, discharging product H2, and making CO and CO2 mixed waste gas enter the shunt layer, and then enter the catalytic oxidation layer and O2 in the air to react.

[0024] The above technical scheme can make full use of the heat generated by the exothermic reaction in the catalytic oxidation layer to supply heat for the endothermic reaction in the reforming reaction layer. In use, methanol and water are respectively metered and mixed, and then sent into a preheater by a feeding pump. After reaching the required reaction temperature through a vaporizer, the mixture is sent into a reactor. Methanol cracking and carbon monoxide shift reactions are simultaneously performed in the fixed-bed catalytic reactor, i.e. CH3OH→CO+2H2 (methanol cracking reaction) and H2O+CO→CO2+H2 (carbon monoxide shift reaction). H2, CO2 and CO are generated. The mixed gas after reaction is sent to a pressure swing adsorption separator through a conversion gas cooling condenser, a gas-liquid separator and a conversion gas purifier. The pressure swing adsorption separator is a pressure swing adsorption system. The pressure swing adsorption system is composed of multiple adsorption towers according to the requirement of gas production. Methanol reforming gas passes through a set of pressure swing adsorption systems operated by multiple adsorbers in parallel. All impurities are separated by one-time adsorption to obtain product hydrogen with a purity of ≥99.999%.

[0025] The methanol and water vapor mixture is mixed by pressurization, and is reformed and converted under the condition of a catalyst and a reaction temperature of 170-300℃ to generate hydrogen and carbon dioxide. The reaction formula is as follows: CH3OH+H2O→CO2+3H2. The technical scheme adopts a mode in which the catalytic oxidation layer and the reforming reaction layer are superposed. The reaction in the methanol reforming reaction layer is CH3OH+H2O→CO2+3H2. This reaction is an endothermic reaction. The catalytic oxidation layer uses two reactions, i.e. H2+O2→H2O and CO+O2→CO2, in the tail gas of the reaction pressure swing adsorption, both of which are exothermic reactions. The reforming reactor and the catalytic reactor are combined in a ring-shaped form. The purpose is to provide as much heat as possible generated by the catalytic reaction to the reforming reaction, increase the contact area of the reaction, and improve the reaction efficiency.

[0026] The preheating vaporizer 3, the methanol reforming reactor and the catalytic oxidation heat conducting oil furnace are integrated, which can increase the specific surface area of the reaction, reduce the required land area and the amount of material of the reactor, save the amount of catalyst used, increase the contact area of the reaction, reduce the contact area with the external environment, reduce the heat loss, reduce the amount of raw material required for catalytic oxidation, and reduce the construction difficulty and cost of the equipment in the construction, installation, debugging and operation processes.

[0027] As shown in Figure 1 and Figure 2 , in the present embodiment, a pair of partitions 5 are vertically arranged in the first shell 4, a current collector cover 7 is arranged between the partitions 5, the outer side of the current collector cover 7, the opposite side of the partitions 5 and the inner side of the first shell 4 jointly form a first catalyst layer, the opposite side of the partitions 5 and the inner side of the current collector cover 7 jointly form a reforming reaction layer, the upper end of the partitions 5 is provided with a current collecting hole 6 connected to the first catalyst layer, and the current collector cover 7 is provided with a first through hole 8 connected to the reforming reaction layer and the first catalyst layer; the lower end of the partitions 5 is provided with a cap cover 9, and the first shell 4 is provided with a center tube 10 penetrating through the first shell 4 and the reactor 1 and forming a high-purity hydrogen outlet 12 at the bottom end.

[0028] The above technical scheme can make the reaction in the reforming reaction layer proceed under catalysis, improve the reaction rate, and the effect diagram is as shown in Figure 2 , wherein the hollow arrow represents the reforming reaction route, and the reactants enter the first catalyst layer after passing through the current collecting hole 6, and the catalyst accelerates the reforming reaction rate.

[0029] As shown in Figure 1 and Figure 2 , in the present embodiment, a second shell 14 is further arranged between the reactor 1 and the first shell 4, a second catalyst layer is formed between the outer side of the second shell 14 and the inner wall of the reactor 1, a catalytic oxidation layer is formed between the inner side of the second shell 14 and the outer side of the first shell 4, and a second through hole 15 is arranged on the surface of the second shell 14 to connect the second catalyst layer and the catalytic oxidation layer; the axial lines of the reactor 1, the first shell 4 and the second shell 14 coincide with each other.

[0030] The above technical scheme can use catalyst to improve the reaction rate in the catalytic oxidation layer, and the catalytic oxidation reaction route is as shown by the solid arrow in Figure 2 , in the reaction process, the reactants in the catalytic oxidation layer will contact the catalyst through the second through hole 15 on the surface of the second shell 14, so as to improve the reaction rate.

[0031] As shown in Figure 2 , in the present embodiment, the preheating vaporizer 3 penetrates through the second catalyst layer and the catalytic oxidation layer in sequence.

[0032] The technical scheme can ensure that the catalytic oxidation reaction in the catalytic oxidation layer can heat and preheat the vaporizer 3.

[0033] As shown in Figure 1 and Figure 2 In the embodiment, the air inlet pipe 16 is arranged obliquely above the reactor 1, the air inlet pipe 16 penetrates through the reactor 1 and is connected to the catalytic oxidation layer, the discharge pipe 17 is arranged obliquely below the second shell 14, and the discharge pipe 17 penetrates through the reactor 1.

[0034] The technical scheme can ensure that the catalytic oxidation reaction in the catalytic oxidation layer can heat and preheat the vaporizer 3.

[0035] Working principle: in use, methanol and water are respectively metered and mixed, then sent into the preheater through a feeding pump, then sent into the reactor after reaching the required reaction temperature through the vaporizer. The methanol cracking and carbon monoxide shift reaction are simultaneously performed in the fixed bed catalytic reactor to generate H2, CO2 and CO. The mixed gas after the reaction is sent to the pressure swing adsorption separator (i.e. a pressure swing adsorption system) through a conversion gas cooling condenser, a gas-liquid separator and a conversion gas purifier. The pressure swing adsorption system is composed of multiple adsorption towers according to the requirement of the gas production amount. The methanol reforming gas passes through a pressure swing adsorption system composed of multiple adsorbers operating in parallel, and all impurities are separated by one-time adsorption to obtain product hydrogen with a purity of ≥99.999%.

[0036] Those skilled in the art will understand that the above discussion of any embodiment is only exemplary and is not intended to suggest that the scope (including claims) of the present application is limited to these examples; under the idea of the present application, the above embodiments or technical features in different embodiments can also be combined, steps can be implemented in any order, and there are many other changes of different aspects of the present application as described above, which are not provided in details for the sake of brevity.

[0037] The present application is intended to cover all such alternatives, modifications and variations as fall within the broad scope of the appended claims. Accordingly, any and all such modifications, variations or equivalents that fall within the spirit and scope of the present application are intended to be included within the scope of the present application.

Claims

1. A methanol reforming and catalytic heating integrated reactor, characterized in that, The application relates to a reactor (1) and a first shell (4) arranged in the reactor (1), a reforming reaction layer is arranged in the first shell (4), the reactor (1) is provided with a methanol raw material liquid feeding pipe (2) communicated with the reforming reaction layer and a high-purity hydrogen outlet (12), a preheating vaporizer (3) is connected to the methanol raw material liquid feeding pipe (2), a catalytic oxidation layer is formed between the reactor (1) and the first shell (4) and used for a catalytic oxidation reaction, the reactor (1) is provided with an air inlet pipe (16) communicated with the catalytic oxidation layer and a discharge pipe (17), the high-purity hydrogen outlet (12) is provided with a separator (11) for separating hydrogen in reforming reaction products, and the high-purity hydrogen outlet (12) is provided with a shunt hole (13) for communicating with the catalytic oxidation layer. A pair of partitions (5) are vertically arranged in the first shell (4), a flow converging cover (7) is arranged between the partitions (5), the outer side of the flow converging cover (7), the opposite sides of the partitions (5) and the inner side of the first shell (4) jointly form a first catalyst layer, the opposite sides of the partitions (5) and the inner side of the flow converging cover (7) jointly form a reforming reaction layer, the upper end of the partition (5) is provided with a flow converging hole (6) connected to the first catalyst layer, and the flow converging cover (7) is provided with a first through hole (8) for connecting the reforming reaction layer and the first catalyst layer.

2. The methanol reforming and catalytic heating integrated reactor according to claim 1, characterized in that, The lower end of the partition (5) is provided with a cap cover (9), a central pipe (10) is arranged in the first shell (4) and penetrates the first shell (4) and the reactor (1) and forms the high-purity hydrogen outlet (12) at the bottom end.

3. The methanol reforming and catalytic heating integrated reactor according to claim 2, characterized in that, The reactor (1) and the first shell (4) are further provided with a second shell (14), a second catalyst layer is formed between the outer side of the second shell (14) and the inner wall of the reactor (1), the inner side of the second shell (14) and the outer side of the first shell (4) form a catalytic oxidation layer, and the surface of the second shell (14) is provided with a second through hole (15) for connecting the second catalyst layer and the catalytic oxidation layer.

4. The methanol reforming and catalytic heating integrated reactor according to claim 3, characterized in that, The preheating vaporizer (3) penetrates the second catalyst layer and the catalytic oxidation layer in sequence, so that the catalytic oxidation reaction in the catalytic oxidation layer can heat the preheating vaporizer (3).

5. The integrated reactor for methanol reforming and catalytic heating according to claim 4, wherein The air inlet pipe (16) is arranged obliquely above the reactor (1), the air inlet pipe (16) penetrates the reactor (1) and connects the catalytic oxidation layer.

6. The integrated reactor for methanol reforming and catalytic heating according to claim 5, wherein The discharge pipe (17) is arranged obliquely below the second shell (14) and penetrates the reactor (1).

7. The integrated reactor for methanol reforming and catalytic heating according to claim 6, wherein The central axes of the reactor (1), the first shell (4) and the second shell (14) coincide with each other.

8. The integrated reactor for methanol reforming and catalytic heating according to claim 4, wherein The separator (11) comprises a converted gas cooling condenser, a gas-liquid separator, a converted gas purifier and a pressure swing adsorption separator.

9. The integrated reactor for methanol reforming and catalytic heating according to claim 1, wherein ​

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