Chemical byproduct gas driven poly-generation system and working method thereof

Abstract

The application provides a chemical byproduct gas driven poly-generation system and a working method thereof, which combines the energy utilization characteristics and resource endowment of a chemical park and a data center park, can safely, efficiently and flexibly utilize various chemical byproduct gases, and realizes gas-cold-heat-electricity-computation multi-energy supply in the chemical-data center integrated park. A pressure swing adsorption device, a membrane separation device and a chemical synthesis device are connected with a byproduct gas pretreatment device; the byproduct gas pretreatment device, a gas analyzer, a flow controller and a gas mixing platform are sequentially connected; a fuel preheater is connected with the gas mixing platform, a gas turbine, a steam turbine and a waste heat boiler; the steam turbine is further connected with a heat source inlet of a generator; the steam turbine is further connected with a heat source inlet of the chemical synthesis device; a heat source outlet of the chemical synthesis device is connected with a water inlet of the waste heat boiler; a heat source outlet of the generator is connected with an inlet of a condenser; a coolant outlet of an evaporator is connected with a coolant inlet of a heat dissipation system.

Description

Technical Field

[0001] This invention relates to a combined heat and power system driven by chemical by-product gas and its operating method, and relates to the field of comprehensive energy utilization technology. Background Technology

[0002] Chemical industrial parks and data center parks, as significant energy consumers, face the dual pressures of energy conservation and emission reduction, as well as improving energy efficiency. Petrochemical and coal chemical production processes generate substantial amounts of byproduct gases, including off-gas from methanol synthesis and Fischer-Tropsch synthesis, PSA purification tail gas from hydrogen purification units, and membrane separation tail gas. Currently, most of these byproduct gases are directly fed into the factory's fuel gas pipeline network as fuel for ordinary boilers, resulting in low utilization efficiency and underutilization of their energy value. Meanwhile, data centers, as high-energy-consuming industries, pose a severe challenge to energy supply due to their enormous electricity and cooling demands.

[0003] Meanwhile, data centers, as a crucial infrastructure in the digital economy era, provide powerful computing capabilities through their server clusters. However, data center operation is inherently an energy-intensive industry, requiring not only a continuous and stable power supply but also efficient cooling systems to ensure normal equipment operation. This supply and demand relationship creates a unique opportunity for industrial synergy: data centers can provide the necessary computing power support for fuel conditioning, while combined cycle systems can provide reliable power supply and cooling capabilities through lithium bromide refrigeration systems.

[0004] Existing technical solutions have significant limitations in terms of system integration, with most research results remaining at the level of local optimization within a single industry sector. For example, patent CN 116731754 A discloses a method and apparatus for efficient coal-based raw material chemical-power cogeneration, which, while achieving chemical-power cogeneration of coal-based energy, suffers from the following shortcomings: First, the system does not consider the dynamic optimization requirements of the fuel characteristics of chemical by-product gas, lacking a real-time monitoring and control mechanism for fuel composition; second, the solution requires the carbon-hydrogen ratio of the fuel gas to be obtained in advance as a fixed parameter, making it difficult to adapt to the dynamic fluctuations in by-product gas composition in actual industrial production; most importantly, the solution completely ignores the supporting role of computing resources in the fuel conditioning process, failing to meet the real-time computing needs of modern industry for conditioning. On the other hand, patent CN120258451 A discloses a collaborative optimization method for a data center integrated energy system with computing-electricity-heat coupling, which, while achieving optimized operation of the data center's internal energy system to some extent, is limited to the data center itself and fails to break through industry boundaries to achieve cross-domain energy-computing collaboration. The solution has the following shortcomings: First, the optimization objective is singular, only considering the energy efficiency improvement of the data center itself, without involving the efficient utilization of external power, cold sources and chemical by-product gas and other energy sources; second, the coordination mechanism is imperfect, lacking two-way energy-information interaction between the chemical park and the data center park; and third, the system architecture is closed, failing to build a cross-industry "energy-resource" cycle system.

[0005] In summary, existing technologies have significant gaps in achieving deep integration of chemical industrial parks and data center parks, and in establishing a complete two-way energy-resource circulation system. Therefore, developing a combined heat and power (CHP) system capable of efficiently and cleanly utilizing chemical by-product gases and meeting the energy needs of data centers not only has significant theoretical innovation value but also provides a practical and feasible technological path for the green and low-carbon development of industrial parks. This cross-industry system integration innovation will drive the transformation and upgrading of energy systems towards intelligence, efficiency, and cleanliness. Summary of the Invention

[0006] The purpose of this invention is to overcome the above-mentioned shortcomings in the existing technology and provide a chemical by-product gas driven multi-generation system and its working method with a reasonable structural design. Combining the energy consumption characteristics and resource endowments of chemical industrial parks and data center parks, it can safely, efficiently and flexibly utilize various chemical by-product gases to realize gas-cooling-heating-electricity-computing multi-energy supply in integrated chemical-data center parks.

[0007] The technical solution adopted by this invention to solve the above problems is: a multi-generation system driven by chemical by-product gas, including a combined cycle cogeneration system, a lithium bromide refrigeration system, and a data center; the combined cycle cogeneration system includes a gas turbine, a waste heat boiler, a steam turbine, and a condenser; the exhaust steam outlet of the steam turbine is connected to the inlet of the condenser, and the outlet of the condenser is connected to the inlet of the waste heat boiler; the exhaust port of the gas turbine is connected to the heat source inlet of the waste heat boiler, and the steam inlet of the steam turbine is connected to the steam outlet of the waste heat boiler; characterized in that: it also includes a chemical by-product gas collection system and a conditioning and blending system; the chemical by-product gas collection system includes a pressure swing adsorption device, a membrane separation device, a chemical synthesis device, and a by-product gas pretreatment device; the pressure swing adsorption device, the membrane separation device, and the chemical synthesis device are all connected to the by-product gas pretreatment device; the conditioning and blending system includes a gas analyzer, a computer control system, and a control system. The system comprises a control platform, a flow controller, and a mixing platform; a by-product gas pretreatment device, a gas analyzer, a flow controller, and a mixing platform are connected in sequence, with the gas analyzer and flow controller both connected to the computing control platform; the combined cycle cogeneration system also includes a fuel preheater; the cold phase inlet of the fuel preheater is connected to the outlet of the mixing platform, the cold phase outlet is connected to the fuel inlet of the gas turbine, the hot phase inlet is connected to the steam extraction port of the steam turbine, and the hot phase outlet is connected to the water inlet of the waste heat boiler; the exhaust steam outlet of the steam turbine is also connected to the heat source inlet of the generator of the lithium bromide refrigeration system; the steam extraction port of the steam turbine is also connected to the heat source inlet of the chemical synthesis unit, and the heat source outlet of the chemical synthesis unit is connected to the water inlet of the waste heat boiler; the heat source outlet of the generator of the lithium bromide refrigeration system is connected to the inlet of the condenser, and the refrigerant outlet of the evaporator is connected to the refrigerant inlet of the data center's cooling system.

[0008] The by-product gas pretreatment device of this invention includes a hydrogen pretreatment device, a membrane separation tail gas pretreatment device, a PSA purification tail gas pretreatment device, a purge gas pretreatment device, and a natural gas pretreatment device; the purge gas outlet of the chemical synthesis unit is connected to the inlet of the purge gas pretreatment device; the PSA purification tail gas outlet of the pressure swing adsorption unit is connected to the inlet of the PSA purification tail gas pretreatment device, and the hydrogen outlet is connected to the inlet of the hydrogen pretreatment device; the hydrogen outlet of the membrane separation unit is connected to the inlet of the hydrogen pretreatment device, and the tail gas outlet is connected to the inlet of the membrane separation tail gas pretreatment device.

[0009] The gas analyzer of the present invention includes a membrane separation tail gas analyzer, a PSA purification tail gas analyzer, and a purge gas analyzer; the inlet of the membrane separation tail gas analyzer is connected to the outlet of the membrane separation tail gas pretreatment device, the inlet of the PSA purification tail gas analyzer is connected to the outlet of the PSA purification tail gas pretreatment device, and the inlet of the purge gas analyzer is connected to the outlet of the purge gas pretreatment device.

[0010] The flow controllers described in this invention include a hydrogen flow controller, a membrane separation tail gas flow controller, a PSA purification tail gas flow controller, a purge gas flow controller, and a natural gas flow controller. The inlet of the hydrogen flow controller is connected to the outlet of the hydrogen pretreatment unit; the inlet of the membrane separation tail gas flow controller is connected to the outlet of the membrane separation tail gas analyzer; the inlet of the PSA purification tail gas flow controller is connected to the outlet of the PSA purification tail gas analyzer; the inlet of the purge gas flow controller is connected to the outlet of the purge gas analyzer; and the inlet of the natural gas flow controller is connected to the outlet of the natural gas pretreatment unit. The outlets of the hydrogen flow controller, membrane separation tail gas flow controller, PSA purification tail gas flow controller, purge gas flow controller, and natural gas flow controller are all connected to the inlet of the mixing platform.

[0011] The combined cycle cogeneration system of the present invention further includes a gas turbine generator and a steam turbine generator, wherein the gas turbine generator is connected to the gas turbine and the steam turbine generator is connected to the steam turbine.

[0012] The outlet of the condenser described in this invention is connected to the inlet of the waste heat boiler via a circulating water pump.

[0013] The combined cycle cogeneration system of the present invention also includes a heating heat exchange device, which is connected to the steam extraction port of the steam turbine.

[0014] The data center and computing control platform described in this invention are connected.

[0015] A method for operating a combined chemical production system driven by chemical by-product gas, characterized by the following steps: The first step is raw material gas collection and pretreatment: hydrogen is purified by a pressure swing adsorption unit and PSA purification tail gas is generated; hydrogen is purified by a membrane separation unit and membrane separation tail gas is generated; chemical synthesis is carried out by a chemical synthesis unit and purge gas is generated; then it is pretreated by a pretreatment unit. The second step is fuel conditioning and blending: the conditioning and blending system monitors the composition and calorific value of each chemical by-product gas in real time through a gas analyzer; the calculation and control platform dynamically calculates the optimal blending ratio based on the preset target calorific value range and Wobbe number range; the flow controller receives instructions from the calculation and control platform to precisely adjust the flow rate of each fuel gas; the mixing platform fully and uniformly mixes multiple fuel gases to output a mixed fuel gas with stable combustion characteristics. The third step is combined heat and power (CHP) and energy cascade utilization: In the combined cycle CHP system, the mixed fuel gas from the mixing platform is preheated by the fuel preheater and then enters the gas turbine for combustion. The exhaust gas from the gas turbine enters the waste heat boiler as a heat source to vaporize water and generate high-temperature steam, which drives the steam turbine. Part of the exhaust steam from the steam turbine enters the lithium bromide refrigeration system for condensation, and the remaining exhaust steam is condensed by the condenser and then sent back to the waste heat boiler for re-vaporization. The steam extracted from the steam turbine can also be used as a heat source for heating the fuel preheater and chemical synthesis unit, and after cooling, it enters the waste heat boiler for re-vaporization. The fourth step is the refrigeration cycle and data center cooling: In the lithium bromide refrigeration system, the exhaust steam from the steam turbine enters the generator to heat the LiBr solution; the refrigerant generated by the evaporator enters the data center's heat dissipation system to cool the data center.

[0016] Compared with the prior art, the present invention has the following advantages and effects: 1. This patent demonstrates significant advantages in comprehensive energy utilization and industrial synergy. Through a sophisticated thermodynamic design of a gas-steam combined cycle, the system achieves efficient conversion of chemical energy from chemical byproducts into electrical energy, effectively reducing power generation costs. The overall energy utilization efficiency reaches over 65%, forming a complete gas-cooling-heating-electricity-computer multi-energy supply system. This multi-energy complementary architecture not only significantly improves comprehensive energy utilization efficiency but also enables the tiered utilization of energy of different grades, providing a complete energy solution for chemical industrial parks and data center parks.

[0017] 2. Utilizing chemical by-product gases in combined cycle cogeneration systems offers significant advantages. First, as byproducts of chemical processes, these gases have relatively low utilization costs, effectively reducing power generation costs. Second, combined cycle systems enable cascaded energy utilization; the high-temperature flue gas from gas turbine power generation can be used to generate steam through a waste heat boiler, driving a steam turbine for secondary power generation. Furthermore, the system can simultaneously meet the electricity, heat, and cooling needs of both chemical industrial parks and data center parks, achieving multi-level integrated energy utilization.

[0018] 3. In terms of fuel adaptability, the real-time monitoring system based on the gas analyzer can control the calorific value fluctuation of the mixed fuel within ±2% and the Wobbe number deviation within ±3%. It can adapt to fuel changes in the full range of hydrogen content from 0% to 100%, effectively solving the problem of interference of chemical by-product gas composition fluctuations on gas turbine operation, greatly expanding the range of fuel applicability, and providing a reliable guarantee for the stable operation of the system.

[0019] 4. An innovative two-way collaborative mechanism between energy and computing power has been established, forming a unique industrial symbiosis model. On the one hand, the combined circulation system provides the data center with a stable power supply and efficient cooling; on the other hand, the data center's computing resources provide real-time computing support for the fuel conditioning system, with computing latency controlled at the millisecond level. This collaborative model of "using electricity to promote computing and using computing to optimize energy" not only improves the overall system performance but also realizes the cyclical and value-added utilization of resources.

[0020] 5. The system's reliability and flexibility are comprehensively enhanced through a multi-layered protection mechanism. The multi-system coupled design architecture allows each subsystem to maintain independent operation while forming a mutually supportive whole. The rapid response characteristics of the intelligent control system enable the system to adapt to different operating conditions, ensuring continuous and stable operation of chemical production and data centers. This design concept provides reliable operational assurance for the industrial park's energy system.

[0021] 6. From an economic perspective, the system significantly reduces the park's energy procurement costs through the resource utilization of coal / petrochemical by-product gas and energy cascade conversion. Simultaneously, the system's internal circulation characteristic reduces dependence on external energy sources, and through self-production and consumption of hydrogen and clean energy substitution, it effectively reduces carbon emission intensity. This design allows the system to achieve significant economic benefits while also demonstrating excellent environmental performance.

[0022] 7. Through the integrated implementation of the above technical solutions, this invention intelligently integrates and reshapes the value of by-product gas and self-produced hydrogen resources in the coal chemical / petrochemical industry. It has significant effects on improving energy utilization efficiency, ensuring system operation safety, and reducing carbon emission intensity, providing an innovative solution for optimizing the energy system of chemical industrial parks. Attached Figure Description

[0023] Figure 1 This is a schematic diagram of the structure of an embodiment of the present invention; Figure 2 This is a flowchart illustrating the workflow of an embodiment of the present invention. Detailed Implementation

[0024] The present invention will be further described in detail below with reference to the accompanying drawings and embodiments. The following embodiments are explanations of the present invention, but the present invention is not limited to the following embodiments.

[0025] I. A chemical by-product gas driven polygeneration system according to an embodiment of the present invention includes a chemical by-product gas collection system 1, a conditioning and blending system 2, a combined cycle cogeneration system 3, a lithium bromide refrigeration system 4, and a data center 5.

[0026] The chemical by-product gas collection system 1 includes a pressure swing adsorption device 101, a membrane separation device 102, a chemical synthesis device 103, and a by-product gas pretreatment device.

[0027] The by-product gas pretreatment unit is responsible for collecting high-purity hydrogen, off-gas, PSA purification tail gas, membrane separation tail gas, and natural gas from the chemical process, and performing necessary pretreatment such as pressurization, dehydration, desulfurization, and preliminary pressure stabilization. The by-product gas pretreatment unit includes a hydrogen pretreatment unit 104, a membrane separation tail gas pretreatment unit 105, a PSA purification tail gas pretreatment unit 106, an off-gas pretreatment unit 107, and a natural gas pretreatment unit 108. The chemical synthesis unit 103 is used for processes such as methanol synthesis or Fischer-Tropsch synthesis, producing hydrogen-rich off-gas as a by-product while generating methanol and high-quality synthetic fuels; the off-gas outlet of the chemical synthesis unit 103 is connected to the inlet of the off-gas pretreatment unit 107. The pressure swing adsorption (PSA) unit 101 is used to purify hydrogen-containing feed gas to produce high-purity hydrogen and generate hydrogen-rich PSA purification tail gas. The PSA purification tail gas outlet of the PSA unit 101 is connected to the inlet of the PSA purification tail gas pretreatment unit 106, and the hydrogen outlet is connected to the inlet of the hydrogen pretreatment unit 104. The membrane separation unit 102 is also used for hydrogen purification, producing high-purity hydrogen while generating membrane separation tail gas with a high methane content. The hydrogen outlet of the membrane separation unit 102 is connected to the inlet of the hydrogen pretreatment unit 104, and the tail gas outlet is connected to the inlet of the membrane separation tail gas pretreatment unit 105.

[0028] The conditioning and blending system 2 includes a gas analyzer, a computational control platform 201, a flow controller, and a gas mixing platform 210.

[0029] The gas analyzers monitor the composition and calorific value of the input by-product gas in real time and transmit the data to the computing and control platform 201. The gas analyzers include a membrane separation tail gas analyzer 202, a PSA purification tail gas analyzer 203, and a purge gas analyzer 204. The inlet of the membrane separation tail gas analyzer 202 is connected to the outlet of the membrane separation tail gas pretreatment unit 105, the inlet of the PSA purification tail gas analyzer 203 is connected to the outlet of the PSA purification tail gas pretreatment unit 106, and the inlet of the purge gas analyzer 204 is connected to the outlet of the purge gas pretreatment unit 107. The flow controllers include a hydrogen flow controller 205, a membrane separation tail gas flow controller 206, a PSA purification tail gas flow controller 207, a purge gas flow controller 208, and a natural gas flow controller 209. The inlet of hydrogen flow controller 205 is connected to the outlet of hydrogen pretreatment unit 104; the inlet of membrane separation tail gas flow controller 206 is connected to the outlet of membrane separation tail gas analyzer 202; the inlet of PSA purification tail gas flow controller 207 is connected to the outlet of PSA purification tail gas analyzer 203; the inlet of purge gas flow controller 208 is connected to the outlet of purge gas analyzer 204; and the inlet of natural gas flow controller 209 is connected to the outlet of natural gas pretreatment unit 108. The gas analyzers and flow controllers are connected to the computational control platform 201. The computational control platform 201 dynamically calculates the optimal blending ratio of hydrogen, natural gas, and the three by-product gases based on the target calorific value range and Wobbe number range for stable combustion of the gas turbine, and generates the mass flow rate setpoint for each fuel gas. The flow controllers receive instructions from the computational control platform 201, adjust the flow rate of each fuel gas in real time, and deliver them to the mixing platform 210 according to the set ratio. The mixing platform 210 thoroughly and uniformly mixes various fuel gases, ultimately outputting a mixed fuel gas with stable and controllable combustion characteristics. The outlets of the hydrogen flow controller 205, membrane separation tail gas flow controller 206, PSA purification tail gas flow controller 207, purge gas flow controller 208, and natural gas flow controller 209 are all connected to the inlet of the mixing platform 210.

[0030] The combined cycle cogeneration system 3 includes a gas turbine, a gas turbine generator 304, a waste heat boiler 305, a fuel preheater 306, a steam turbine 307, a steam turbine generator 308, a condenser 309, a circulating water pump 310, and a heating heat exchange device 311.

[0031] The gas turbine includes a compressor 301, a combustion chamber 302, and a gas turbine 303. A gas turbine generator 304 is connected to the gas turbine. The exhaust port of the gas turbine 303 is connected to the heat source inlet of the waste heat boiler 305. The cold phase inlet of the fuel preheater 306 is connected to the outlet of the mixing platform 210, the cold phase outlet is connected to the fuel inlet of the combustion chamber 302 of the gas turbine, the hot phase inlet is connected to the extraction port of the steam turbine 307, and the hot phase outlet is connected to the water inlet of the waste heat boiler 305. The steam turbine 307 is connected to a steam turbine generator 308. The steam inlet of the steam turbine 307 is connected to the steam outlet of the waste heat boiler 305. The exhaust steam outlet of the steam turbine 307 is connected to the heat source inlet of the generator 401 of the lithium bromide refrigeration system 4 and the inlet of the condenser 309. The outlet of the condenser 309 is connected to the water inlet of the waste heat boiler 305 via a circulating water pump 310. The inlet of the heating heat exchanger 311 is connected to the extraction port of the steam turbine 307. The extraction port of the steam turbine 307 is also connected to the heat source inlet of the chemical synthesis unit 103, and the heat source outlet of the chemical synthesis unit 103 is connected to the water inlet of the waste heat boiler 305. The conditioned mixed fuel gas is sent to the combustion chamber 302 of the gas turbine for combustion to generate power, driving the generator to produce electricity; the high-temperature flue gas discharged from the gas turbine enters the waste heat boiler 305 to heat water and generate steam, which in turn drives the steam turbine 307 to generate electricity, forming a high-efficiency combined cycle. The electricity generated by this system is mainly used to power the chemical plants and server cluster 502 in the chemical-data center park, and prioritizes powering the feed gas compressors of the PSA purification unit and membrane separation unit 102. Part of the exhaust steam generated after the steam turbine 307 performs work enters the lithium bromide refrigeration system 4 as a driving heat source. After releasing heat in the lithium bromide system, it is condensed. The remaining exhaust steam is condensed by the condenser and finally sent back to the waste heat boiler 305 for reheating by the circulating water pump. Part of the high-temperature steam generated by this system can also be used for fuel preheating and process heating of the chemical synthesis unit 103, as well as to provide heating for the park through the heating heat exchange device, thereby realizing the cascade and comprehensive utilization of energy.

[0032] The lithium bromide refrigeration system 4 includes a generator 401, a condenser 402, a throttling device 403, an evaporator 404, an absorber 405, and a solution pump 406. The generator 401 is connected to the condenser 402, the condenser 402 is connected to the evaporator 404 via the throttling device 403, the evaporator 404 is connected to the absorber 405, and the absorber 405 is connected to the generator 401 via the solution pump 406. The heat source outlet of the generator 401 is connected to the inlet of the condenser 309. The refrigerant outlet of the evaporator 404 is connected to the heat dissipation system 501. The refrigerant import connection.

[0033] Data center 5 includes a cooling system 501, a server cluster 502, and a power supply system 503. The cooling system 501 uses the cold source generated by the lithium bromide refrigeration system 4 as the main cooling method; the power supply system 503 mainly relies on the power generated by the gas-steam combined cycle system; the server cluster 502 provides real-time computing power support for the computing control platform 201 in the conditioning and blending system 2, ensuring the fuel conditioning response speed, while the surplus computing power can also provide services to the outside world, forming synergy and value-added computing power resources within the system.

[0034] II. The working method of the chemical by-product gas driven polygeneration system according to the present invention includes the following steps: The first step is the collection and pretreatment of raw gas: hydrogen is purified by the pressure swing adsorption (PSA) device 101 in the chemical by-product gas collection system 1, producing PSA purification tail gas; hydrogen is purified by the membrane separation device 102, producing membrane separation tail gas; and chemical synthesis is carried out by the chemical synthesis device 103, producing purge gas. Subsequently, various gases are pretreated by pressurization, dehydration, desulfurization, and pressure stabilization through the hydrogen pretreatment device 104, the membrane separation tail gas pretreatment device 105, the PSA purification tail gas pretreatment device 106, the purge gas pretreatment device 107, and the natural gas pretreatment device 108, respectively.

[0035] The second step is fuel conditioning and blending: The conditioning and blending system 2 monitors the composition and calorific value of each chemical by-product gas in real time through the membrane separation tail gas analyzer 202, the PSA purification tail gas analyzer 203, and the purge gas analyzer 204; the calculation and control platform 201 dynamically calculates the optimal blending ratio according to the preset target calorific value range and the Wobbe number range to ensure that the system can operate stably under the blending ratio; the hydrogen flow controller 205, the membrane separation tail gas flow controller 206, the PSA purification tail gas flow controller 207, the purge gas flow controller 208, and the natural gas flow controller 209 receive instructions from the calculation and control platform 201 to accurately adjust the flow rate of each fuel gas; the mixing platform 210 fully and uniformly mixes the various fuel gases and outputs a mixed fuel gas with stable combustion characteristics. When the gas turbine combustor 302 used has poor adaptability to hydrogen, an upper limit for the proportion of fuel hydrogen can be set, with natural gas as the main fuel and chemical by-product gas as an auxiliary fuel for conditioning, in order to ensure the stability of the system; when the gas turbine combustor 302 used has strong adaptability to hydrogen, even if the fuel is pure hydrogen, good stability can be guaranteed, and chemical by-product gas can be used as the main fuel for conditioning.

[0036] The third step, combined heat and power (CHP) and energy cascade utilization: In the combined cycle CHP system 3, compressor 301 draws in and compresses air. The mixed fuel gas from mixing platform 210 is preheated by fuel preheater 306 and then enters combustion chamber 302 to react with compressed air. The resulting high-temperature gas drives gas turbine 303 to drive gas turbine generator 304 to generate electricity. The exhaust gas from the gas turbine enters waste heat boiler 305 as a heat source to vaporize water and generate high-temperature steam, which drives steam turbine 307 to drive steam generator 304. Steam turbine generator 308 generates electricity; the exhaust steam from steam turbine 307 is partially condensed in a lithium bromide refrigeration system, while the remaining exhaust steam is condensed in condenser 309 and then sent back to waste heat boiler 305 for re-vaporization via circulating water pump 310; heating heat exchange device 311 utilizes steam extracted from steam turbine 307 to provide heating for the park; steam extracted from steam turbine 307 can also be used as a heat source for fuel preheater 306 and chemical synthesis unit 103, and after cooling, it enters waste heat boiler 305 for re-heating and vaporization. The steam temperature range required by chemical synthesis unit 103 is 370K~500K, and the pressure range is 0.1MPa~2.5MPa. The electricity generated by gas turbine generator 304 and steam turbine generator 308 supplies pressure swing adsorption unit 101, membrane separation unit 102, and data center server cluster 502, respectively, with surplus electricity supplying other chemical units in the park.

[0037] The fourth step, refrigeration cycle and data center cooling: In the lithium bromide refrigeration system 4, exhaust steam from the steam turbine enters the generator 401 to heat the LiBr solution, causing the refrigerant to vaporize and enter the condenser 402. The remaining concentrated LiBr solution returns to the absorber 405. The gaseous refrigerant releases heat and condenses into a liquid state in the condenser 402. After being depressurized and cooled by the throttling device 403, it enters the evaporator 404. In the evaporator 404, the liquid refrigerant vaporizes into a low-pressure gaseous state, while absorbing heat from the medium being cooled, generating a refrigeration effect. The refrigerant generated by the evaporator 404 dissipates heat for the server cluster 502 through the heat dissipation system 501 of the data center 5. In the absorber 405, the concentrated LiBr solution continuously absorbs the low-pressure gaseous refrigerant generated by the evaporator 404 to maintain the low-pressure environment within the evaporator 404. The LiBr refrigerant solution formed after the concentrated LiBr solution absorbs the refrigerant is pressurized by the solution pump 406 and sent back to the generator 401, completing the refrigeration cycle. The required steam temperature range for the lithium bromide refrigeration system 4 is 370K~440K, and the pressure range is 0.03MPa~0.7MPa.

[0038] Fifth step, computing power support and energy feedback: The server cluster 502 of data center 5 obtains power supply through data center power supply system 503 and relies on the cold source provided by lithium bromide cooling system 4 to ensure operating temperature. At the same time, it provides real-time computing power support for the computing control platform 201 in conditioning and blending system 2. While ensuring the fuel conditioning response speed, the surplus computing power also provides services to the outside world, forming the synergy and value-added of computing power resources within the system.

[0039] Furthermore, it should be noted that the specific embodiments described in this specification may differ in the shape and name of their components, etc. The above description is merely illustrative of the structure of the present invention. All equivalent or simple variations made based on the structure, features, and principles described in this patent concept are included within the protection scope of this patent. Those skilled in the art can make various modifications or additions to the described specific embodiments or use similar methods to substitute them, as long as they do not deviate from the structure of the present invention or exceed the scope defined by the claims, all of which should fall within the protection scope of this invention.

Claims

1. A multi-generation system driven by chemical by-product gas, comprising a combined cycle cogeneration system, a lithium bromide refrigeration system, and a data center; the combined cycle cogeneration system comprising a gas turbine, a waste heat boiler, a steam turbine, and a condenser; the exhaust steam outlet of the steam turbine is connected to the inlet of the condenser, and the outlet of the condenser is connected to the inlet of the waste heat boiler; the exhaust port of the gas turbine is connected to the heat source inlet of the waste heat boiler, and the steam inlet of the steam turbine is connected to the steam outlet of the waste heat boiler; characterized in that: It also includes a chemical by-product gas collection system and a conditioning and blending system; the chemical by-product gas collection system includes a pressure swing adsorption unit, a membrane separation unit, a chemical synthesis unit, and a by-product gas pretreatment unit; the pressure swing adsorption unit, the membrane separation unit, and the chemical synthesis unit are all connected to the by-product gas pretreatment unit; the conditioning and blending system includes a gas analyzer, a computational control platform, a flow controller, and a gas mixing platform; The by-product gas pretreatment unit, gas analyzer, flow controller, and mixing platform are connected in sequence. Both the gas analyzer and flow controller are connected to the computing control platform. The combined cycle cogeneration system also includes a fuel preheater. The cold phase inlet of the fuel preheater is connected to the outlet of the mixing platform, the cold phase outlet is connected to the fuel inlet of the gas turbine, the hot phase inlet is connected to the steam extraction port of the steam turbine, and the hot phase outlet is connected to the water inlet of the waste heat boiler. The exhaust steam outlet of the steam turbine is also connected to the heat source inlet of the generator of the lithium bromide refrigeration system. The steam extraction port of the steam turbine is also connected to the heat source inlet of the chemical synthesis unit, and the heat source outlet of the chemical synthesis unit is connected to the water inlet of the waste heat boiler. The heat source outlet of the generator of the lithium bromide refrigeration system is connected to the inlet of the condenser, and the refrigerant outlet of the evaporator is connected to the refrigerant inlet of the data center's cooling system.

2. The chemical by-product gas-driven polygeneration system according to claim 1, characterized in that: The by-product gas pretreatment device includes a hydrogen pretreatment device, a membrane separation tail gas pretreatment device, a PSA purification tail gas pretreatment device, a purge gas pretreatment device, and a natural gas pretreatment device; the purge gas outlet of the chemical synthesis unit is connected to the inlet of the purge gas pretreatment device; the PSA purification tail gas outlet of the pressure swing adsorption unit is connected to the inlet of the PSA purification tail gas pretreatment device, and the hydrogen outlet is connected to the inlet of the hydrogen pretreatment device; the hydrogen outlet of the membrane separation unit is connected to the inlet of the hydrogen pretreatment device, and the tail gas outlet is connected to the inlet of the membrane separation tail gas pretreatment device.

3. The chemical by-product gas-driven polygeneration system according to claim 2, characterized in that: The gas analyzer includes a membrane separation tail gas analyzer, a PSA purification tail gas analyzer, and a purge gas analyzer; the inlet of the membrane separation tail gas analyzer is connected to the outlet of the membrane separation tail gas pretreatment device, the inlet of the PSA purification tail gas analyzer is connected to the outlet of the PSA purification tail gas pretreatment device, and the inlet of the purge gas analyzer is connected to the outlet of the purge gas pretreatment device.

4. The chemical by-product gas-driven polygeneration system according to claim 3, characterized in that: The flow controllers include a hydrogen flow controller, a membrane separation tail gas flow controller, a PSA purification tail gas flow controller, a purge gas flow controller, and a natural gas flow controller. The inlet of the hydrogen flow controller is connected to the outlet of the hydrogen pretreatment unit; the inlet of the membrane separation tail gas flow controller is connected to the outlet of the membrane separation tail gas analyzer; the inlet of the PSA purification tail gas flow controller is connected to the outlet of the PSA purification tail gas analyzer; the inlet of the purge gas flow controller is connected to the outlet of the purge gas analyzer; and the inlet of the natural gas flow controller is connected to the outlet of the natural gas pretreatment unit. The outlets of the hydrogen flow controller, membrane separation tail gas flow controller, PSA purification tail gas flow controller, purge gas flow controller, and natural gas flow controller are all connected to the inlet of the mixing platform.

5. The chemical by-product gas-driven polygeneration system according to claim 1, characterized in that: The combined cycle cogeneration system also includes a gas turbine generator and a steam turbine generator, with the gas turbine generator connected to the gas turbine and the steam turbine generator connected to the steam turbine.

6. The chemical by-product gas-driven polygeneration system according to claim 1, characterized in that: The outlet of the condenser is connected to the inlet of the waste heat boiler via a circulating water pump.

7. The chemical by-product gas-driven polygeneration system according to claim 1, characterized in that: The combined cycle cogeneration system also includes a heating heat exchange device, which is connected to the steam extraction port of the steam turbine.

8. The chemical by-product gas-driven polygeneration system according to claim 1, characterized in that: The data center is connected to the computing control platform.

9. A method of operating a multi-product system driven by chemical by-product gas as described in any one of claims 1-8, characterized in that: Includes the following steps: The first step is raw material gas collection and pretreatment: hydrogen is purified by a pressure swing adsorption unit and PSA purification tail gas is generated; hydrogen is purified by a membrane separation unit and membrane separation tail gas is generated; chemical synthesis is carried out by a chemical synthesis unit and purge gas is generated; then it is pretreated by a pretreatment unit. The second step is fuel conditioning and blending: the conditioning and blending system monitors the composition and calorific value of each chemical by-product gas in real time through a gas analyzer; The calculation and control platform dynamically calculates the optimal blending ratio based on the preset target calorific value range and Wobbe number range; the flow controller receives instructions from the calculation and control platform to precisely adjust the flow rate of each fuel gas; the mixing platform fully and uniformly mixes multiple fuel gases and outputs mixed fuel gas with stable combustion characteristics. The third step is combined heat and power (CHP) and energy cascade utilization: In the combined cycle CHP system, the mixed fuel gas from the mixing platform is preheated by the fuel preheater and then enters the gas turbine for combustion. The exhaust gas from the gas turbine enters the waste heat boiler as a heat source to vaporize water and generate high-temperature steam, which drives the steam turbine. Part of the exhaust steam from the steam turbine enters the lithium bromide refrigeration system for condensation, and the remaining exhaust steam is condensed by the condenser and then sent back to the waste heat boiler for re-vaporization. The steam extracted from the steam turbine can also be used as a heat source for heating the fuel preheater and chemical synthesis unit, and after cooling, it enters the waste heat boiler for re-vaporization. The fourth step is the refrigeration cycle and data center cooling: In the lithium bromide refrigeration system, the exhaust steam from the steam turbine enters the generator to heat the LiBr solution; the refrigerant generated by the evaporator enters the data center's heat dissipation system to cool the data center.

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