Miniaturized equipment for converting biomass gas into methanol

Abstract

The utility model provides miniaturized equipment for converting biomass gas into methanol. The utility model relates to miniaturized equipment for converting biomass gas into methanol. Comprising a biomass gas pretreatment reactor, a thermocatalytic conversion reactor, a condensation heat exchange unit, a feed gas recombination reactor, a first pressurization unit, a carbon reduction and hydrogen extraction reactor, a second pressurization unit, a molecular deconstruction reactor, a preheating unit, a high-pressure directional reconstruction reactor, a PSA decarbonization reactor and a gradient spiral condensation unit which are connected in sequence, the thermocatalytic conversion reactor is connected with a purified water preparation operation unit, and a gas path outlet of the gradient spiral condensation unit is connected with the first pressurization unit. According to the utility model, the difference of utilization facilities can be perfectly solved, the limitation of time and space is overcome, the methanol can be used immediately after being produced, the complexity of conversion in the intermediate process is eliminated, and the required important product methanol is obtained in one step.

Description

Technical Field

[0001] The utility model relates to the technical field of methanol preparation, and more specifically to a miniaturized device for converting biomass gas into methanol. Background Art

[0002] The application prospects of biomass gas to methanol are very broad, especially in terms of energy utilization and environmental protection. Currently, with the increasing demand for energy and the intensification of environmental problems, more and more countries and companies are beginning to pay attention to the application and development of biomass gas to methanol.

[0003] There are still some problems with existing biomass gas utilization technology and related equipment. First, the equipment scale of existing technology is too large and can only perform large-scale processing, so it cannot meet the processing needs of sustainable raw material biomass gas. Second, the existing biomass gas processing technology and equipment conditions have minimum operating restrictions, and there is no better small equipment that can perform corresponding flexible processing.

[0004] Therefore, developing a set of efficient miniaturized equipment for converting biomass gas into methanol has far-reaching significance for my country's current national conditions. Utility Model Content

[0005] To achieve the above objectives, the present invention provides a miniaturized biomass gas to methanol conversion device. This device perfectly addresses the differences in utilization facilities, overcomes time and space limitations, and allows for immediate production and immediate use, eliminating the tedious intermediate conversion process and providing the desired important product, methanol, in one step.

[0006] In order to solve the above technical problems, the technical solution adopted by the utility model is: a miniaturized biomass gas to methanol conversion equipment, which includes a biomass gas pretreatment reactor, a thermal catalytic conversion reactor, a condensation heat exchange unit, a raw gas recombination reactor, a first boosting unit, a carbon reduction and hydrogen extraction reactor, a second boosting unit, a molecular deconstruction reactor, a preheating unit, a high-pressure directional reconstruction reactor, a PSA decarbonization reactor and a gradient spiral condensation unit connected in sequence; the thermal catalytic conversion reactor is connected to a pure water preparation operation unit, and the gas outlet of the gradient spiral condensation unit is connected to the first boosting unit.

[0007] When the equipment is in operation, the biomass gas (mainly composed of 3000-5000ppm H2S, 55% CH4, and 45% CO2) is pumped through the power equipment to the biomass gas pretreatment reactor for pretreatment to remove some unnecessary impurities, resulting in purified biomass gas (mainly composed of CH4, with a content of approximately 99%). This gas then enters the thermal catalytic conversion reactor for the first catalytic reaction, during which pure water is added and heated to convert the purified biomass gas into the first synthesis gas (mainly composed of H2O, H2, CH4, CO, and CO2). Since purified water is required for the first catalytic reaction of the purified biomass gas in the thermal catalytic conversion reactor, the purified water preparation operation unit connected to the thermal catalytic conversion reactor can provide a sufficient amount of purified water for the reaction. The converted high-temperature first synthesis gas is cooled to a lower temperature, generally around 30°C, by a condensation heat exchange unit to precipitate the water therein. The synthesis gas with water removed then enters the raw gas reforming reactor for CH4 autothermal reforming to generate a second synthesis gas (main components are H2, CH4 and CO, with a ratio of approximately CO:H2:CH4=3.15:9.25:0.1); the second synthesis gas is pressurized to the reaction pressure (2.5MPa) by the first booster unit and then enters the carbon reduction and hydrogen extraction reactor to separate a part of the CO and most of the CH4, with the remaining CO being about 20% and CH4 being about 0.5%). The separated permeate gas is discharged through the permeate gas outlet of the carbon reduction and hydrogen extraction reactor, and the separated residual gas passes through the second booster unit to separate the second synthesis gas. After the generated gas is pressurized to 3.5-5.5MPa, it enters the molecular deconstruction reactor. Under the action of the high-pressure deconstruction catalyst, a part of the CO and H2 in the retentate gas are deconstructed into methanol precursor ions (CHO*). The deconstructed gas (CO:H2:CHO*:CO2=24:62.8:10:1) obtained after deconstruction enters the preheating unit through the power equipment and is preheated to the reaction temperature. Then it enters the high-pressure directional reconstruction reactor to carry out carbon oxide hydrogenation to produce alcohol to obtain methanol. The mixture after the reaction enters the PSA decarbonization reactor for decarbonization operation to remove excess C. Finally, the products in the mixture are condensed and separated by the gradient spiral condensation unit. After separation, methanol and water are automatically discharged as products. The unreacted gas after separation enters the first boosting unit for reuse.

[0008] Furthermore, the biomass gas pretreatment reactor includes a drying unit, a decarbonization unit, and a desulfurization unit connected in series. The drying unit removes a small amount of moisture from the biomass gas, while the decarbonization and desulfurization units remove H2S and CO2 from the biomass gas, resulting in the purified biomass gas primarily consisting of CH4. The drying, decarbonization, and desulfurization units are designed with one unit in use and one in reserve to ensure effective decarbonization and desulfurization.

[0009] Furthermore, the condensation heat exchange unit includes a waste heat recovery heat exchanger and a water cooling heat exchanger connected in series, the thermal catalytic conversion reactor is connected to the waste heat recovery heat exchanger, the water cooling heat exchanger is connected to the raw gas recombination reactor, and the liquid outlets of the waste heat recovery heat exchanger and the water cooling heat exchanger are both connected to the thermal catalytic conversion reactor. In this way, a two-stage condensation heat exchange is adopted. The purpose of the waste heat recovery heat exchanger as the first stage of condensation heat exchange is mainly to achieve heat recovery, and the recovered heat can be used for other purposes; the purpose of the water cooling heat exchanger as the second stage of condensation heat exchange is to perform deep cooling of the product, thereby achieving the recovery of excess water and separation of product gas. After separation, the excess water is circulated into the front-end thermal catalytic conversion reactor for reuse to avoid waste.

[0010] Furthermore, the gradient spiral condensation unit includes a first gradient spiral condensation heat exchanger and a second gradient condensation heat exchanger connected in series, and the PSA decarbonization reactor is connected to the first gradient spiral condensation heat exchanger. Similarly, the first gradient spiral condensation heat exchanger is used to recover heat, while the second gradient condensation heat exchanger is used for targeted product recovery, thereby achieving methanol and water recovery and separation of unreacted gas.

[0011] The present invention also includes a cooling water reserve unit and a cold water operation unit. The cooling water reserve unit is respectively connected to the condensing water inlet of the waste heat recovery heat exchanger, the water cooling heat exchanger, the first gradient spiral condensing heat exchanger, and the second gradient condensing heat exchanger. The condensing water outlet of the waste heat recovery heat exchanger, the water cooling heat exchanger, the first gradient spiral condensing heat exchanger, and the second gradient condensing heat exchanger is connected to one end of the cold water operation unit, and the other end of the cold water operation unit is connected to the cooling water reserve unit. The cooling water reserve unit is mainly used to provide the cooling water required for deep cooling for the entire system, and the cold water operation unit is mainly used to heat and cool the condensed water after heat exchange to ensure the cooling effect of the condensed water recycling.

[0012] Furthermore, the pure water preparation operation unit includes a pure water preparation system and a pure water storage system that are interconnected. The pure water storage system is connected to the thermal catalytic conversion reactor through a metering and conveying device to provide a sufficient amount of pure water for the subsequent thermal catalytic conversion reaction.

[0013] As a preferred embodiment, a combustion heating unit is further connected between the biomass gas pretreatment reactor and the thermal catalytic conversion reactor, and the combustion heating unit is also connected to the preheating unit. In this way, the combustion heating unit can simultaneously provide the necessary heat for the thermal catalytic conversion reactor and the preheating unit. The purified biomass gas (CH4 content of approximately 99%) after being treated in the biomass gas pretreatment reactor is divided into two parts. One part (accounting for approximately 50% of the total gas volume) enters the combustion heating unit as fuel for combustion, providing heat for the thermal catalytic conversion reactor and the preheating unit; the other part (accounting for approximately 50% of the total gas volume) is used as the reaction gas for the thermal catalytic conversion.

[0014] The present invention also includes an electrical control system for controlling the biomass gas pretreatment reactor, the thermal catalytic conversion reactor, the condensation heat exchange unit, the raw gas reforming reactor, the first boosting unit, the carbon reduction and hydrogen extraction reactor, the second boosting unit, the molecular deconstruction reactor, the preheating unit, the high-pressure directional reconstruction reactor, the PSA decarbonization reactor and the gradient spiral condensation unit, as well as providing them with electrical energy.

[0015] In the present invention, the thermal catalytic conversion reactor adopts the operation mode of water-methane wet reforming, and the hydrogen-carbon ratio of the obtained first synthesis gas is about 2.6:1, which meets the requirements of molecular deconstruction reaction to produce methanol and unconverted gas recovery.

[0016] In the present invention, the biomass gas is a mixed gas of H2S, CH4 and CO2.

[0017] Compared with the prior art, the present invention has the following beneficial effects:

[0018] This utility model provides a miniaturized biomass gas-to-methanol conversion device. This device perfectly addresses the differences in utilization facilities, overcoming time and space constraints. It produces methanol immediately, eliminating the tedious intermediate conversion process and providing the desired important product, methanol, in a single step. Furthermore, the miniaturized device features modularity, allowing it to be combined according to varying production capacities to meet diverse application requirements. BRIEF DESCRIPTION OF THE DRAWINGS

[0019] Figure 1 It is a schematic diagram of the overall structure of Example 1 of the present utility model.

[0020] Figure 2 It is a schematic diagram of the overall structure of Example 2 of the present utility model. DETAILED DESCRIPTION

[0021] The drawings are for illustrative purposes only and should not be construed as limiting this patent. To better illustrate the embodiments, some components in the drawings may be omitted, enlarged, or reduced in size, and do not represent actual product dimensions. Those skilled in the art will understand that some well-known structures and their descriptions may be omitted from the drawings. The positional relationships depicted in the drawings are for illustrative purposes only and should not be construed as limiting this patent.

[0022] Example 1

[0023] like Figure 1 As shown, a miniaturized device for converting biomass gas to methanol includes a biomass gas pretreatment reactor 1, a thermal catalytic conversion reactor 2, a condensation heat exchange unit 3, a raw gas recombination reactor 4, a first booster unit 5, a carbon reduction and hydrogen extraction reactor 6, a second booster unit 7, a molecular deconstruction reactor 8, a preheating unit 9, a high-pressure directional reconstruction reactor 10, a PSA decarbonization reactor 11 and a gradient spiral condensation unit 12, which are connected in sequence; a pure water preparation operation unit 13 is connected to the thermal catalytic conversion reactor 2, and the gas outlet of the gradient spiral condensation unit 12 is connected to the first booster unit 5.

[0024] When the device is in operation, the biomass gas (mainly composed of 3000-5000ppm H2S, 55% CH4, and 45% CO2) is pumped through the power equipment to the biomass gas pretreatment reactor 1 for pretreatment to remove some unnecessary impurities and obtain purified biomass gas (mainly composed of CH4, with a content of about 99%); then it enters the thermal catalytic conversion reactor 2 for the first catalytic reaction. During the catalytic reaction, pure water needs to be added and heated to convert the purified biomass gas into the first synthesis gas (mainly composed of H2O, H2, CH4, CO, and CO2). Since pure water is required for the first catalytic reaction of the purified biomass gas in the thermal catalytic conversion reactor 2, the pure water preparation operation unit 13 connected to the thermal catalytic conversion reactor 2 can provide a sufficient amount of pure water for the reaction. The converted high-temperature first synthesis gas is cooled to a lower temperature, generally around 30°C, by the condensation heat exchange unit 3 to precipitate the water therein. The synthesis gas with water removed then enters the raw gas reforming reactor 4 for CH4 autothermal reforming to generate the second synthesis gas (main components are H2, CH4 and CO, with a ratio of approximately CO:H2:CH4=3.15:9.25:0.1); the second synthesis gas is pressurized to the reaction pressure (2.5MPa) by the first booster unit 5 and then enters the carbon reduction and hydrogen extraction reactor 6 to separate a part of the CO and most of the CH4, with the remaining CO being about 20% and CH4 being about 0.5%). The separated permeate gas is discharged through the permeate gas outlet of the carbon reduction and hydrogen extraction reactor 6, and the separated residual gas passes through the second booster unit 7 to convert the second synthesis gas After being pressurized to 3.5-5.5 MPa, it enters the molecular deconstruction reactor 8, where a portion of the CO and H2 in the retentate gas are deconstructed into methanol precursor ions (CHO*) under the action of a high-pressure deconstruction catalyst. The deconstructed gas (CO:H2:CHO*:CO2=24:62.8:10:1) obtained after deconstruction passes through a power device and enters a preheating unit 9 to be preheated to the reaction temperature. It then enters a high-pressure directional reconstruction reactor 10 to carry out a carbon oxide hydrogenation to alcohol reaction to obtain methanol. The mixture after the reaction enters a PSA decarbonization reactor 11 for decarbonization operation to remove excess C. Finally, the product in the mixture is condensed and separated by a gradient spiral condensation unit 12. After separation, methanol and water are automatically discharged as products. The unreacted gas after separation enters the first boosting unit 5 for reuse.

[0025] In this embodiment, the biomass gas pretreatment reactor 1 includes a drying unit, a decarbonization unit, and a desulfurization unit connected in series. The drying unit removes a small amount of moisture from the biomass gas, while the decarbonization and desulfurization units remove H2S and CO2 from the biomass gas, resulting in the purified biomass gas primarily consisting of CH4. The drying, decarbonization, and desulfurization units are designed with one unit in use and one in reserve to ensure effective decarbonization and desulfurization.

[0026] like Figure 1 As shown, the condensation heat exchange unit 3 includes a waste heat recovery heat exchanger 31 and a water cooling heat exchanger 32 connected in series. The thermal catalytic conversion reactor 2 is connected to the waste heat recovery heat exchanger 31, and the water cooling heat exchanger 32 is connected to the feed gas recombination reactor 4. The liquid outlets of the waste heat recovery heat exchanger 31 and the water cooling heat exchanger 32 are both connected to the thermal catalytic conversion reactor 2. In this way, a two-stage condensation heat exchange is adopted. The purpose of the waste heat recovery heat exchanger 31 as the first stage of condensation heat exchange is mainly to achieve heat recovery, and the recovered heat can be used for other purposes; the purpose of the water cooling heat exchanger 32 as the second stage of condensation heat exchange is to deep cool the product, thereby achieving excess water recovery and product gas separation. After separation, the excess water is recycled into the front-end thermal catalytic conversion reactor 2 for reuse to avoid waste.

[0027] In this embodiment, the gradient spiral condensation unit 12 includes a first gradient spiral condensation heat exchanger and a second gradient condensation heat exchanger connected in series, and the PSA decarbonization reactor 11 is connected to the first gradient spiral condensation heat exchanger. Similarly, the purpose of the first gradient spiral condensation heat exchanger is to achieve heat recovery, while the purpose of the second gradient condensation heat exchanger is to achieve targeted product recovery, thereby achieving methanol and water recovery and separation of unreacted gas.

[0028] This embodiment also includes a cooling water reserve unit and a cold water operation unit. The cooling water reserve unit is connected to the condensing water inlet of the waste heat recovery heat exchanger 31, the water cooling heat exchanger 32, the first gradient spiral condensing heat exchanger, and the second gradient condensing heat exchanger, respectively. The condensing water outlets of the waste heat recovery heat exchanger 31, the water cooling heat exchanger 32, the first gradient spiral condensing heat exchanger, and the second gradient condensing heat exchanger are all connected to one end of the cold water operation unit, and the other end of the cold water operation unit is connected to the cooling water reserve unit. The cooling water reserve unit primarily provides the cooling water necessary for deep cooling of the entire system, while the cold water operation unit primarily exchanges heat and cools the condensed water after heat exchange to ensure the cooling effect of the condensed water recycling.

[0029] In this embodiment, the pure water preparation operation unit 13 includes a pure water preparation system and a pure water storage system that are interconnected. The pure water storage system is connected to the thermal catalytic conversion reactor 2 through a metering and conveying device to provide a sufficient amount of pure water for the subsequent thermal catalytic conversion reaction.

[0030] In this embodiment, the thermal catalytic conversion reactor 2 adopts the operation mode of water-methane wet reforming, and the hydrogen-carbon ratio of the obtained first synthesis gas is about 2.6:1, which meets the requirements of molecular deconstruction reaction to produce methanol and unconverted gas recovery.

[0031] Example 2

[0032] This embodiment is similar to embodiment 1, except that Figure 2As shown, a combustion heating unit 14 is also connected between the biomass gas pretreatment reactor 1 and the thermal catalytic conversion reactor 2, and the combustion heating unit 14 is also connected to the preheating unit 9. In this way, the combustion heating unit 14 can provide the necessary heat for the thermal catalytic conversion reactor 2 and the preheating unit 9 at the same time. The purified biomass gas (CH4 content of about 99%) after being treated by the biomass gas pretreatment reactor 1 is divided into two parts. One part (accounting for about 50% of the total gas volume) enters the combustion heating unit 14 as fuel for combustion, providing heat for the thermal catalytic conversion reactor 2 and the preheating unit 9; the other part (accounting for about 50% of the total gas volume) is used as a reaction gas for thermal catalytic conversion. The structure and working principle of the other parts of this embodiment are the same as those of Example 1.

[0033] Example 3

[0034] This embodiment is similar to Example 2, except that it further includes an electronic control system for controlling the biomass gas pretreatment reactor 1, the thermal catalytic conversion reactor 2, the condensation heat exchange unit 3, the raw gas reforming reactor 4, the first booster unit 5, the carbon reduction and hydrogen extraction reactor 6, the second booster unit 7, the molecular deconstruction reactor 8, the preheating unit 9, the high-pressure directional reconstruction reactor 10, the PSA decarbonization reactor 11, and the gradient spiral condensation unit 12, as well as providing electrical energy thereto. The structure and working principle of the remaining parts of this embodiment are the same as those of Example 2.

[0035] Obviously, the above embodiments of the present invention are merely examples for the purpose of clearly illustrating the present invention, and are not intended to limit the implementation methods of the present invention. A person skilled in the art will be able to make other variations or modifications based on the above description. It is not necessary and impossible to enumerate all implementation methods here. Any modifications, equivalent substitutions, and improvements made within the spirit and principles of the present invention shall be included within the scope of protection of the claims of the present invention.

Claims

1. A miniaturized biomass gas to methanol conversion device, characterized in that: The invention comprises a biomass gas pretreatment reactor (1), a thermal catalytic conversion reactor (2), a condensation heat exchange unit (3), a raw gas recombination reactor (4), a first booster unit (5), a carbon reduction and hydrogen extraction reactor (6), a second booster unit (7), a molecular deconstruction reactor (8), a preheating unit (9), a high-pressure directional reconstruction reactor (10), a PSA decarbonization reactor (11) and a gradient spiral condensation unit (12) which are connected in sequence; the thermal catalytic conversion reactor (2) is connected to a pure water preparation operation unit (13), and the gas outlet of the gradient spiral condensation unit (12) is connected to the first booster unit (5).

2. The miniaturized biomass gas to methanol conversion device according to claim 1, characterized in that: The biomass gas pretreatment reactor (1) comprises a drying unit, a decarbonization unit and a desulfurization unit connected in series.

3. The miniaturized biomass gas to methanol conversion device according to claim 1, characterized in that: The condensing heat exchange unit (3) includes a waste heat recovery heat exchanger (31) and a water cooling heat exchanger (32) connected in series, the thermal catalytic conversion reactor (2) is connected to the waste heat recovery heat exchanger (31), the water cooling heat exchanger (32) is connected to the raw gas reforming reactor (4), and the liquid outlets of the waste heat recovery heat exchanger (31) and the water cooling heat exchanger (32) are both connected to the thermal catalytic conversion reactor (2).

4. The miniaturized biomass gas to methanol conversion device according to claim 3, characterized in that: The gradient spiral condensing unit (12) comprises a first gradient spiral condensing heat exchanger and a second gradient condensing heat exchanger connected in series, and the PSA decarbonization reactor (11) is connected to the first gradient spiral condensing heat exchanger.

5. The miniaturized biomass gas to methanol conversion device according to claim 4, characterized in that: It also includes a cooling water reserve unit and a cold water operation unit, wherein the cooling water reserve unit is respectively connected to the water inlet ends of the condensing water circuit of the waste heat recovery heat exchanger (31), the water cooling heat exchanger (32), the first gradient spiral condensing heat exchanger and the second gradient condensing heat exchanger, and the water outlet ends of the condensing water circuit of the waste heat recovery heat exchanger (31), the water cooling heat exchanger (32), the first gradient spiral condensing heat exchanger and the second gradient condensing heat exchanger are all connected to one end of the cold water operation unit, and the other end of the cold water operation unit is connected to the cooling water reserve unit.

6. The miniaturized biomass gas to methanol conversion device according to claim 1, characterized in that: The pure water preparation operation unit (13) comprises a pure water preparation system and a pure water storage system which are connected to each other, and the pure water storage system is connected to the thermal catalytic conversion reactor (2) via a metering and conveying device.

7. The miniaturized biomass gas to methanol conversion device according to claim 1, characterized in that: A combustion heating unit (14) is also connected between the biomass gas pretreatment reactor (1) and the thermal catalytic conversion reactor (2), and the combustion heating unit (14) is also connected to the preheating unit (9).

8. The miniaturized biomass gas to methanol conversion device according to claim 1, characterized in that: It also includes an electric control system for controlling the biomass gas pretreatment reactor (1), the thermal catalytic conversion reactor (2), the condensation heat exchange unit (3), the raw gas reforming reactor (4), the first boosting unit (5), the carbon reduction and hydrogen extraction reactor (6), the second boosting unit (7), the molecular deconstruction reactor (8), the preheating unit (9), the high-pressure directional reconstruction reactor (10), the PSA decarbonization reactor (11) and the gradient spiral condensation unit (12), as well as providing them with electrical energy.

9. The miniaturized biomass gas to methanol conversion device according to claim 1, characterized in that: The thermal catalytic conversion reactor (2) adopts the operation mode of water-methane wet reforming.

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