A process flow structure for hydrogen co-production with cement admixture from high oil content and high calcium oil sand

Abstract

The application discloses a hydrogen production and cement admixture co-production process structure of high-oil and high-calcium oil sand, and belongs to the technical field of energy and chemical industry. The process structure is composed of an oil gas production system of oil sand and heat carrier mixing pyrolysis, a rich hydrogen gas system of oil gas and steam reforming and carbon dioxide absorption, a hydrogen production system of rich hydrogen gas heat recovery, dust removal and purification, a calcium carbonate in oil sand temperature rising decomposition and calcium oxide absorption carbon dioxide circulation system, a flue gas energy recovery and dust removal system and a cement admixture collection system. The oil gas produced by oil sand pyrolysis directly enters an oil gas reforming reactor to generate a rich hydrogen gas by reforming reaction and calcium oxide absorption carbon dioxide reaction, and hydrogen is obtained by further purification. The calcium carbonate in oil sand and calcium oxide conversion circulation promote hydrogen generation, and are output as cement admixture products. The application realizes hydrogen production and cement admixture co-production of oil sand through multi-system coupling.

Description

Technical Field

[0001] This application relates to a process flow structure for the co-production of cement admixtures from high-oil-content and high-calcium-content oil sands for hydrogen production, belonging to the field of energy and chemical technology. Background Technology

[0002] Oil sands are sands or sandstones containing natural bitumen, a mixture of natural bitumen and minerals. The natural bitumen (the "oil" in oil sands) is the most valuable component; the higher its content, the greater its utilization value. As an unconventional oil and gas resource, oil sands have abundant reserves and wide distribution globally. The composition of oil sands varies from region to region. High-oil-content (usually referring to extractable oil exceeding 13%) and high-calcium-content (high proportion of calcium in the minerals) oil sands are one type. For example, the oil sands from Buton Island in Indonesia can achieve an oil extraction rate of up to 25%, with calcium carbonate accounting for over 70% of their mineral chemical composition. This high oil content expands the scope of oil sand utilization, making hydrogen production possible. Typically, the proportion of minerals in oil sands is greater than that of organic matter (natural bitumen). This portion of the minerals must meet ecological and environmental protection requirements for the exploitation and utilization of oil sands to have practical value. Based on the characteristics of different types of oil sands, suitable processes are developed with the goal of achieving economic and social benefits through the comprehensive utilization of the organic matter (natural bitumen) and minerals in oil sands. High-calcium oil sands are more meaningful because their calcium content plays a role in the transformation of organic matter (natural bitumen) into more valuable products (e.g., promoting hydrogen generation and increasing hydrogen production), and can also be exported as a valuable product, such as as a cement admixture in building materials. Utility Model Content

[0003] To address the challenge of resource utilization of high-oil-content and high-calcium-content oil sands, this application provides a technical solution that couples a process flow structure for hydrogen production and cement admixture co-production from high-oil-content and high-calcium-content oil sands, thereby realizing hydrogen production and cement admixture co-production from oil sands.

[0004] The technical solution adopted in this application is as follows:

[0005] According to one aspect of this application, a process flow structure for producing hydrogen from high-oil and high-calcium oil sands and co-producing cement admixtures is provided. The process flow structure comprises an oil sands and heat carrier mixing and pyrolysis system for producing oil and gas, an oil and gas steam reforming system for absorbing carbon dioxide to generate hydrogen-rich gas, a hydrogen-rich gas heat recovery, dust removal, and purification system, a system for heating and decomposing calcium carbonate in the oil sands and circulating calcium oxide to absorb carbon dioxide, a flue gas energy recovery and dust removal system, and a cement admixture collection system.

[0006] Optionally, the oil sand and heat carrier mixed pyrolysis oil and gas production system includes an oil sand crusher 2, an oil sand storage tank 3, an oil sand sealed conveyor belt 4, a mixer 5, and an oil sand pyrolysis reactor 6.

[0007] The inlet of the oil sand crusher 2 is connected to the input pipeline of the raw material oil sand 1, the outlet of the oil sand crusher 2 is connected to the inlet of the oil sand storage tank 3, the outlet of the oil sand storage tank 3 is located at the feed end of the oil sand sealing conveyor belt 4, the discharge end of the conveyor belt 4 is located at the first inlet of the mixer 5, and the outlet of the mixer 5 is connected to the inlet of the oil sand pyrolysis reactor 6.

[0008] The upper outlet of the oil sand pyrolysis reactor 6 is connected to the lower part of the oil and gas reforming reactor 7 in the oil and gas steam reforming system for absorbing carbon dioxide and generating hydrogen-rich gas. The second inlet of the mixer 5 is connected to the first outlet of the high-temperature heat carrier storage tank 13 in the oil sand heating and decomposition system for calcium carbonate and calcium oxide for absorbing carbon dioxide.

[0009] Raw oil sand 1 is processed by oil sand crusher 2 to a particle size range of 0-10mm and sent to oil sand storage tank 3 for later use. The oil sand enters mixer 5 via oil sand sealed conveyor belt 4, where it is mixed with heat carrier from high temperature (800-850℃) heat carrier storage tank 13 and a pyrolysis reaction is initiated. Mixer 5 adopts a double helix structure and controls the temperature at 450-500℃. The generated oil gas and oil sand semi-coke (the residual solids after oil sand pyrolysis, containing residual carbon) enter oil sand pyrolysis reactor 6 together to complete the pyrolysis. Reaction oil sand pyrolysis reactor 6 adopts a moving bed, with materials flowing from top to bottom and the temperature controlled at 450-500℃. The generated oil gas enters oil gas reforming reactor 7.

[0010] Optionally, the oil and gas steam reforming system for absorbing carbon dioxide to generate hydrogen-rich gas includes an oil and gas reforming reactor 7, a primary feed control U valve 9 for calcium oxide powder, a secondary feed control U valve 10 for calcium oxide powder, a primary feed switch slide valve 11 for calcium oxide powder, a secondary feed switch slide valve 12 for calcium oxide powder, a cyclone separator for calcium carbonate powder 25, and a circulation control U valve 26 for calcium carbonate powder.

[0011] The upper part of the oil and gas reforming reactor 7 is connected to the inlet of the calcium carbonate powder cyclone separator 25 through an insulated pipe. The lower outlet of the calcium carbonate powder cyclone separator 25 is connected to the lower part of the oil and gas reforming reactor 7 through an insulated pipe equipped with a calcium carbonate powder circulation control U valve 26. The secondary feed switch slide valve 12 and the secondary feed control U valve 10 of calcium oxide powder are sequentially installed on the secondary feed pipe in the upper part of the oil and gas reforming reactor 7. The primary feed switch slide valve 11 and the primary feed control U valve 9 of calcium oxide powder are sequentially installed on the primary feed pipe in the lower part of the oil and gas reforming reactor 7.

[0012] The oil and gas reforming reactor 7 is connected to the second outlet of the high-temperature heat carrier storage tank 13 in the calcium carbonate heating and decomposition and calcium oxide carbon dioxide absorption circulation system in the oil sands through a primary feed pipe and a secondary feed pipe. The upper outlet of the calcium carbonate powder cyclone separator 25 is connected to the upper inlet of the steam preheater 27 in the hydrogen-rich gas heat recovery, dust removal and purification hydrogen production system.

[0013] The oil sands pyrolysis reactor 6 is connected to the oil and gas reforming reactor 7 via an insulated pipe. The oil and gas produced by the oil sands pyrolysis reactor 6 enters the oil and gas reforming reactor 7 and undergoes a reforming reaction with water vapor to produce hydrogen and carbon monoxide. The oil and gas reforming reactor 7 adopts a fluidized bed configuration and controls the temperature at 650-700℃. Simultaneously, a water-gas shift reaction and a reaction in which calcium oxide absorbs carbon dioxide to produce calcium carbonate occur, causing the water-gas shift reaction to proceed in a direction that favors the production of more hydrogen. The oil and gas reforming reactor 7 is connected to the calcium carbonate powder cyclone separator 25 via an insulated pipe to recover the calcium carbonate powder carried out by the hydrogen-rich gas from the reaction, including unreacted calcium oxide powder. The calcium carbonate powder is circulated through the calcium carbonate powder circulation control valve 26 to maintain the stability of the fluidized bed in the oil and gas reforming reactor 7.

[0014] Optionally, the hydrogen-rich gas heat recovery dust removal and purification hydrogen production system includes a steam preheater 27, a hydrogen-rich gas waste heat boiler 28, a hydrogen-rich gas primary cyclone separator 29, a hydrogen-rich gas secondary cyclone separator 30, a hydrogen-rich gas bag filter 31, a hydrogen-rich gas compressor 34, a hydrogen separation waste gas fan 43, and a hydrogen purification separator 35.

[0015] The lower outlet of the steam preheater 27 is connected to the upper inlet of the hydrogen-rich gas waste heat boiler 28. The upper part of the steam preheater 27 is provided with a steam inlet. The lower outlet of the hydrogen-rich gas waste heat boiler 28 is connected to the upper side of the hydrogen-rich gas primary cyclone separator 29. The upper end of the hydrogen-rich gas primary cyclone separator 29 is connected to the upper side of the hydrogen-rich gas secondary cyclone separator 30. The upper end of the hydrogen-rich gas secondary cyclone separator 30 is connected to the upper side of the hydrogen-rich gas tertiary cyclone separator 31. The upper end of the hydrogen-rich gas bag filter 31 is connected to the upper side of the hydrogen purification separator 35 through a pipe with a hydrogen separation waste gas fan 43. The lower side of the hydrogen purification separator 35 is provided with a hydrogen outlet.

[0016] The upper end of the hydrogen purification separator 35 is connected to the upper side of the steam preheater 27 and the first inlet of the riser supplement burner 41 in the calcium carbonate heating and decomposition and calcium oxide carbon dioxide absorption circulation system in the oil sand through a pipe with a hydrogen separation residual gas fan 43.

[0017] The hydrogen-rich gas produced by the high-temperature (650-700℃) reaction is processed through a steam preheater 27 and a hydrogen-rich gas waste heat boiler 28 for waste heat utilization. After dust removal by a primary hydrogen-rich gas cyclone separator 29, a secondary hydrogen-rich gas cyclone separator 30, and a hydrogen-rich gas bag filter 31, the gas is pressurized by a hydrogen-rich gas compressor 34 and enters a hydrogen purification separator 35 to obtain product hydrogen 36. The hydrogen purification separator 35 uses membrane separation to control the product hydrogen concentration to be greater than 99%. The residual gas (methane, carbon monoxide, carbon dioxide) separated by the hydrogen purification separator 35 is pressurized by a hydrogen separation residual gas fan 43. A portion of the hydrogen separation residual gas (refueling) 39 is used to supplement the burner 41 in the riser pipe, releasing heat to replenish the energy of the riser pipe 8. The other portion of the hydrogen separation residual gas (recirculation) 38 is used for heat exchange in the steam preheater 27 and is used to supplement the fluidizing gas in the oil and gas reforming reactor 7.

[0018] Optionally, the calcium carbonate heating and decomposition and calcium oxide carbon dioxide absorption circulation system in the oil sand includes a riser pipe 8, a high-temperature heat carrier storage tank 13, a heat carrier cyclone separator 14, and a riser pipe supplementary burner 41.

[0019] The lower end of the riser pipe 8 is connected to the outlet end of the riser pipe supplementary burner 41, the lower outlet end of the oil sand pyrolysis reactor 6 in the oil sand and heat carrier mixed pyrolysis oil and gas production system, the lower outlet end of the oil and gas reforming reactor 7 in the oil and gas steam reforming system for absorbing carbon dioxide to generate hydrogen-rich gas, and the side outlet end of the air preheater 16 in the flue gas energy recovery and dust removal system. The upper end of the riser pipe 8 is connected to the upper end of the heat carrier cyclone separator 14. The lower end of the heat carrier cyclone separator 14 is connected to the upper end of the high-temperature heat carrier storage tank 13. The upper end of the heat carrier cyclone separator 14 is connected to the upper end of the air preheater 16 in the flue gas energy recovery and dust removal system. The lower end of the riser pipe 8 is provided with a discharge outlet for cement admixture calcium slag.

[0020] The calcium carbonate generated by the oil and gas steam reforming system, which absorbs carbon dioxide to produce hydrogen-rich gas, enters riser 8. Simultaneously, the semi-coke from the oil sands pyrolysis reactor 6 and the heat carrier enter riser 8 together. Inside riser 8, the residual carbon in the semi-coke and the residual carbon adsorbed on the heat carrier from the oil and gas reforming reactor 7 and the oil sands pyrolysis reactor 6 burn to provide energy for heating the heat carrier and decomposing calcium carbonate into calcium oxide and carbon dioxide. At the same time, the riser supplementary burner 41 provides energy supplementation. Riser 8 adopts an airflow bed form, with the material flowing from bottom to top. The temperature is controlled at 800-850℃, decomposing into calcium oxide and carbon dioxide. After passing through the riser and the heat carrier cyclone separator 14, the material enters the high-temperature heat carrier storage tank 13 to begin a new reaction regeneration cycle.

[0021] Optionally, the flue gas energy recovery and dust removal system includes an air preheater 16, a flue gas waste heat boiler 17, a primary flue gas cyclone separator 18, a secondary flue gas cyclone separator 19, a flue gas bag filter 20, and a flue gas exhaust fan 21.

[0022] The air preheater 16 is provided with an air inlet at its upper part. The lower end of the air preheater 16 is connected to the upper end of the flue gas waste heat boiler 17. The lower end of the flue gas waste heat boiler 17 is connected to the upper side of the primary flue gas cyclone separator 18. The upper end of the primary flue gas cyclone separator 18 is connected to the upper side of the secondary flue gas cyclone separator 19. The upper end of the secondary flue gas cyclone separator 19 is connected to the upper side of the flue gas bag filter 20. The upper end of the flue gas bag filter 20 is connected to the flue gas exhaust fan 21.

[0023] The flue gas generated from combustion in riser 8 is separated into heat carriers by heat carrier cyclone separator 14 and enters air preheater 16 and flue gas waste heat boiler 17 to recover heat. After passing through flue gas primary cyclone separator 18, flue gas secondary cyclone separator 19 and flue gas bag filter 20, calcium oxide powder is collected as a cement admixture product. At the same time, the flue gas is discharged by flue gas exhaust fan 21. The air preheated by air preheater 16 (temperature 400-500℃) is partly used as combustion aid 40 in riser supplementary burner 41 and partly enters riser 8 as combustion aid for residual carbon.

[0024] Optionally, the cement admixture collection system includes a cement admixture calcium oxide collector 24 and a cement admixture calcium carbonate collector 32.

[0025] The upper end of the cement admixture calcium oxide collector 24 is connected to the lower end of the primary flue gas cyclone separator 18, the secondary flue gas cyclone separator 19, and the flue gas bag filter 20 in the flue gas energy recovery dust removal system. The lower end of the cement admixture calcium oxide collector 24 is provided with an outlet for the mud admixture calcium oxide powder 23.

[0026] The upper end of the cement admixture calcium carbonate collector 32 is connected to the lower end of the hydrogen-rich gas primary cyclone separator 29, the hydrogen-rich gas secondary cyclone separator 30, and the hydrogen-rich gas bag filter 31 in the hydrogen-rich gas heat recovery dust removal and purification hydrogen production system. The lower end of the cement admixture calcium carbonate collector 32 is provided with a cement admixture calcium carbonate powder 33 discharge port.

[0027] The cement admixture product is collected by a hydrogen-rich gas primary cyclone separator 29, a hydrogen-rich gas secondary cyclone separator 30, and a hydrogen-rich gas bag filter 31. The flue gas generated by combustion in the riser pipe 8 passes through a heat carrier cyclone separator 14 to separate the heat carrier, which then enters an air preheater 16 and a flue gas waste heat boiler 17 to recover heat. Calcium oxide powder is collected by a flue gas primary cyclone separator 18, a flue gas secondary cyclone separator 19, and a flue gas bag filter 20, and is used as a cement admixture product. Cement admixture calcium slag 42 (heat carrier particles that cannot be lifted, including calcium carbonate particles and calcium oxide particles) is collected and discharged from the bottom of the riser pipe 8, and is used as a cement admixture product.

[0028] The beneficial effects that this application can produce include:

[0029] The process flow structure for producing cement admixtures from high-oil and high-calcium oil sands through hydrogen production is provided in this application. Through multi-system coupling, it realizes the co-production of cement admixtures from hydrogen production from oil sands. The oil and gas produced by the pyrolysis of oil sands directly enter the oil and gas reforming reactor, where a reforming reaction occurs. At the same time, calcium oxide absorbs carbon dioxide to generate hydrogen-rich gas, which is further purified to obtain hydrogen. The conversion and recycling of calcium carbonate and calcium oxide in the oil sands promotes the generation of hydrogen, which is then output as a cement admixture product. Attached Figure Description

[0030] Figure 1 This is a schematic diagram of the process flow for the co-production of cement admixtures from high-oil and high-calcium oil sands for hydrogen production in this application.

[0031] Attached Figure Labels

[0032] 1. Raw material oil sand; 2. Oil sand crusher; 3. Oil sand storage tank;

[0033] 4. Oil sand sealing conveyor belt; 5. Mixer; 6. Oil sand pyrolysis reactor;

[0034] 7. Oil and gas reforming reactor; 8. Riser; 9. U-valve for primary feed control of calcium oxide powder;

[0035] 10. U-valve for secondary feed control of calcium oxide powder; 11. Slide valve for primary feed switch of calcium oxide powder;

[0036] 12. Secondary feed switch slide valve for calcium oxide powder; 13. High-temperature heat carrier storage tank;

[0037] 14. Heat carrier cyclone separator; 15. Air; 16. Air preheater;

[0038] 17. Flue gas waste heat boiler; 18. Flue gas primary cyclone separator;

[0039] 19. Two-stage cyclone separator for flue gas; 20. Flue gas bag filter; 21. Flue gas exhaust fan;

[0040] 22. Flue gas; 23. Cement admixture calcium oxide powder; 24. Cement admixture calcium oxide powder collector;

[0041] 25. Calcium carbonate powder cyclone separator; 26. Calcium carbonate powder circulation control U-valve;

[0042] 27. Steam preheater; 28. Hydrogen-rich gas waste heat boiler;

[0043] 29. Hydrogen-rich gas primary cyclone separator; 30. Hydrogen-rich gas secondary cyclone separator;

[0044] 31. Hydrogen-rich gas bag filter; 32. Cement admixture calcium carbonate powder collector;

[0045] 33. Cement admixture calcium carbonate powder; 34. Hydrogen-rich gas compressor; 35. Hydrogen purification separator;

[0046] 36. Hydrogen; 37. Water vapor; 38. Hydrogen separation residue (recycled);

[0047] 39. Hydrogen separation residual gas (re-combustion); 40. Preheated air; 41. Riser supplementary burner;

[0048] 42. Cement admixture calcium slag; 43. Hydrogen separation waste gas blower; 44. Hydrogen-rich gas. Detailed Implementation

[0049] The present application is described in detail below with reference to the embodiments, but the present application is not limited to these embodiments.

[0050] Unless otherwise specified, all raw materials used in the embodiments of this application were purchased through commercial channels.

[0051] According to one embodiment of this application, a process flow structure for the co-production of cement admixtures from high-oil-content and high-calcium-content oil sands for hydrogen production comprises: an oil sands and heat carrier mixing and pyrolysis system for producing oil and gas; an oil and gas steam reforming system for absorbing carbon dioxide to generate hydrogen-rich gas; a hydrogen-rich gas heat recovery, dust removal, and purification system; a system for heating and decomposing calcium carbonate in the oil sands and circulating it with calcium oxide to absorb carbon dioxide; a flue gas energy recovery and dust removal system; and a cement admixture collection system. Its structural schematic diagram is shown below. Figure 1As shown, the oil sand and heat carrier mixed pyrolysis oil and gas production system includes raw oil sand 1, oil sand crusher 2, oil sand storage tank 3, oil sand sealed conveyor belt 4, mixer 5, and oil sand pyrolysis reactor 6. The outlet of mixer 5 is connected to oil sand pyrolysis reactor 6. The raw oil sand 1 is processed by oil sand crusher 2, with a particle size range of 0-10mm, and sent to oil sand storage tank 3 for later use. The oil sand enters mixer 5 through oil sand sealed conveyor belt 4, and is mixed with heat carrier from high temperature (800-850℃) heat carrier storage tank 13 to initiate pyrolysis reaction. Mixer 5 adopts a double helix structure and controls the temperature at 450-500℃. The generated oil and gas and oil sand semi-coke (the residual solid after oil sand pyrolysis, containing residual carbon) enter oil sand pyrolysis reactor (6) together to complete pyrolysis. The reaction oil sand pyrolysis reactor 6 adopts a moving bed, with materials flowing from top to bottom and the temperature controlled at 450-500℃. The generated oil and gas enter oil and gas reforming reactor 7.

[0052] Furthermore, the oil and gas steam reforming system for absorbing carbon dioxide and generating hydrogen-rich gas includes an oil and gas reforming reactor 7, a primary feed control U-valve 9 for calcium oxide powder, a secondary feed control U-valve 10 for calcium oxide powder, a primary feed switch slide valve 11 for calcium oxide powder, a secondary feed switch slide valve 12 for calcium oxide powder, a calcium carbonate powder cyclone separator 25, a calcium carbonate powder circulation control U-valve 26, steam 37, and hydrogen separation residual gas (circulation) 38. An oil sands pyrolysis reactor 6 is connected to the oil and gas reforming reactor 7 via an insulated pipe. The oil and gas generated by the oil sands pyrolysis reactor 6 enters the oil and gas reforming reactor 7 and reacts with the steam... The oil and gas reforming reactor 7, employing a fluidized bed configuration and controlled at 650-700℃, undergoes a water-gas shift reaction and a reaction where calcium oxide absorbs carbon dioxide to form calcium carbonate. This process directs the water-gas shift reaction towards a higher hydrogen production rate. The oil and gas reforming reactor 7 is connected to a calcium carbonate powder cyclone separator 25 via an insulated pipe. This separator recovers the calcium carbonate powder carried away by the hydrogen-rich gas from the reaction, including unreacted calcium oxide powder. Circulation is achieved through a calcium carbonate powder circulation control valve 26, maintaining the stability of the fluidized bed in the oil and gas reforming reactor 7.

[0053] Furthermore, the calcium carbonate heating and decomposition system in the oil sands and the calcium oxide carbon dioxide absorption circulation system includes a riser pipe 8, a high-temperature heat carrier storage tank 13, a heat carrier cyclone separator 14, a riser pipe supplementary burner 41, air 15, preheated air 40, and hydrogen separation residual gas (supplementary combustion) 39. Calcium carbonate generated by the oil-gas steam reforming system for absorbing carbon dioxide to generate hydrogen-rich gas enters the riser pipe 8. Simultaneously, semi-coke from the oil sands in the oil sands pyrolysis reactor 6 and the heat carrier enter the riser pipe 8 together. Inside the riser pipe 8, residual carbon in the semi-coke from the oil sands and residual carbon adsorbed on the heat carrier from the oil-gas reforming reactor 7 and the oil sands pyrolysis reactor 6 burn to provide energy for heating the heat carrier and decomposing calcium carbonate into calcium oxide and carbon dioxide. At the same time, the riser pipe supplementary burner 41 provides energy supplementation. The riser pipe 8 adopts an airflow bed form, with materials flowing from bottom to top at a controlled temperature of 800-850℃, decomposing into calcium oxide and carbon dioxide. After passing through the riser and heat carrier cyclone separator 14, the materials enter the high-temperature heat carrier storage tank 13 to begin a new reaction regeneration cycle.

[0054] Furthermore, the hydrogen-rich gas heat recovery, dust removal, and purification hydrogen production system includes a steam preheater 27, a hydrogen-rich gas waste heat boiler 28, a hydrogen-rich gas primary cyclone separator 29, a hydrogen-rich gas secondary cyclone separator 30, a hydrogen-rich gas bag filter 31, hydrogen-rich gas 44, a hydrogen-rich gas compressor 34, a hydrogen separation waste gas fan 43, a hydrogen purification separator 35, and product hydrogen 36. The high-temperature (650-700℃) reaction product hydrogen-rich gas, after waste heat utilization by the steam preheater 27 and the hydrogen-rich gas waste heat boiler 28, passes through the hydrogen-rich gas primary cyclone separator 29 and the hydrogen-rich gas secondary cyclone separator 30. The gas is collected by a hydrogen-rich gas bag filter 31, pressurized by a hydrogen-rich gas compressor 34, and then enters a hydrogen purification separator 35 to obtain product hydrogen. The hydrogen purification separator 35 uses a membrane separation method to control the concentration of product hydrogen to be greater than 99%. The residual gas (methane, carbon monoxide, carbon dioxide) separated by the hydrogen purification separator 35 is pressurized by a hydrogen separation residual gas fan 43. Part of the hydrogen separation residual gas (re-combustion) 39 is used to supplement the burner 41 in the riser pipe, where combustion releases heat and supplements the energy of the riser pipe 8. The other part of the hydrogen separation residual gas (recirculation) 38 is heat-exchanged by a steam preheater 27 and used to supplement the fluidizing gas in the oil and gas reforming reactor 7.

[0055] Furthermore, the flue gas energy recovery and dust removal system includes an air preheater 16, a flue gas waste heat boiler 17, a primary flue gas cyclone separator 18, a secondary flue gas cyclone separator 19, a flue gas bag filter 20, a flue gas exhaust fan 21, and flue gas 22. The flue gas generated from combustion in the riser pipe 8 passes through the heat carrier cyclone separator 14 to separate the heat carrier, and then enters the air preheater 16 and the flue gas waste heat boiler 17 to recover heat. After passing through the primary flue gas cyclone separator 18, the secondary flue gas cyclone separator 19, and the flue gas bag filter 20, calcium oxide powder is collected as a cement admixture product. At the same time, the flue gas 22 is discharged by the flue gas exhaust fan 21. The air preheated by the air preheater 16 (temperature 400-500℃) is partly used as a combustion aid 40 in the supplementary burner 41 of the riser pipe, and partly enters the riser pipe 8 as a combustion aid for residual carbon combustion.

[0056] Furthermore, the cement admixture collection system includes a hydrogen-rich gas primary cyclone separator 29, a hydrogen-rich gas secondary cyclone separator 30, a hydrogen-rich gas bag filter 31, a cement admixture calcium carbonate collector 32, a flue gas primary cyclone separator 18, a flue gas secondary cyclone separator 19, a flue gas bag filter 20, a cement admixture calcium oxide collector 24, and a cement admixture calcium slag 42. The cement admixture product is obtained by collecting the cement admixture through the hydrogen-rich gas primary cyclone separator 29, the hydrogen-rich gas secondary cyclone separator 30, and the hydrogen-rich gas bag filter 31. The flue gas generated by combustion in the riser pipe 8 passes through the heat carrier cyclone separator 14 to separate the heat carrier, and enters the air preheater 16 and the flue gas waste heat boiler 17 to recover heat. The calcium oxide powder is collected by the flue gas primary cyclone separator 18, the flue gas secondary cyclone separator 19, and the flue gas bag filter 20 as the cement admixture product. The bottom of the riser pipe 8 collects and discharges cement admixture calcium slag 42 (non-liftable heat carrier particles, including calcium carbonate particles and calcium oxide particles), which is used as a cement admixture product.

[0057] Example 1

[0058] A schematic diagram of the process flow for the co-production of cement admixtures from high-oil and high-calcium oil sands for hydrogen production is shown below. Figure 1 As shown, the equipment name, connecting pipeline or product name is indicated by labels 1-44 in the attached figures.

[0059] The process flow structure for producing hydrogen from high-oil and high-calcium oil sands and co-producing cement admixtures consists of an oil sands and heat carrier mixing and pyrolysis system for producing oil and gas, an oil and gas steam reforming system for absorbing carbon dioxide to generate hydrogen-rich gas, a hydrogen-rich gas heat recovery, dust removal and purification system, a calcium carbonate in oil sands heating and decomposition system and a calcium oxide carbon dioxide absorption circulation system, a flue gas energy recovery and dust removal system, and a cement admixture collection system.

[0060] The oil sand and heat carrier mixed pyrolysis oil and gas production system includes an oil sand crusher 2, an oil sand storage tank 3, an oil sand sealed conveyor belt 4, a mixer 5, and an oil sand pyrolysis reactor 6;

[0061] The inlet of the oil sand crusher 2 is connected to the input pipeline of the raw material oil sand 1, the outlet of the oil sand crusher 2 is connected to the inlet of the oil sand storage tank 3, the outlet of the oil sand storage tank 3 is located at the feed end of the oil sand sealing conveyor belt 4, the discharge end of the conveyor belt 4 is located at the first inlet of the mixer 5, and the outlet of the mixer 5 is connected to the inlet of the oil sand pyrolysis reactor 6.

[0062] The upper outlet of the oil sand pyrolysis reactor 6 is connected to the lower part of the oil and gas reforming reactor 7 in the oil and gas steam reforming system for absorbing carbon dioxide and generating hydrogen-rich gas. The second inlet of the mixer 5 is connected to the first outlet of the high-temperature heat carrier storage tank 13 in the oil sand heating and decomposition system for calcium carbonate and calcium oxide for absorbing carbon dioxide.

[0063] The oil and gas steam reforming system for absorbing carbon dioxide to generate hydrogen-rich gas includes an oil and gas reforming reactor 7, a primary feed control U valve 9 for calcium oxide powder, a secondary feed control U valve 10 for calcium oxide powder, a primary feed switch slide valve 11 for calcium oxide powder, a secondary feed switch slide valve 12 for calcium oxide powder, a cyclone separator for calcium carbonate powder 25, and a circulation control U valve 26 for calcium carbonate powder.

[0064] The upper part of the oil and gas reforming reactor 7 is connected to the inlet of the calcium carbonate powder cyclone separator 25 through an insulated pipe. The lower outlet of the calcium carbonate powder cyclone separator 25 is connected to the lower part of the oil and gas reforming reactor 7 through an insulated pipe equipped with a calcium carbonate powder circulation control U valve 26. The secondary feed switch slide valve 12 and the secondary feed control U valve 10 of calcium oxide powder are sequentially installed on the secondary feed pipe in the upper part of the oil and gas reforming reactor 7. The primary feed switch slide valve 11 and the primary feed control U valve 9 of calcium oxide powder are sequentially installed on the primary feed pipe in the lower part of the oil and gas reforming reactor 7.

[0065] The oil and gas reforming reactor 7 is connected to the second outlet of the high-temperature heat carrier storage tank 13 in the calcium carbonate heating and decomposition and calcium oxide carbon dioxide absorption circulation system in the oil sands through a primary feed pipe and a secondary feed pipe. The upper outlet of the calcium carbonate powder cyclone separator 25 is connected to the upper inlet of the steam preheater 27 in the hydrogen-rich gas heat recovery, dust removal and purification hydrogen production system.

[0066] The hydrogen-rich gas heat recovery, dust removal, and purification hydrogen production system includes a steam preheater 27, a hydrogen-rich gas waste heat boiler 28, a hydrogen-rich gas primary cyclone separator 29, a hydrogen-rich gas secondary cyclone separator 30, a hydrogen-rich gas bag filter 31, a hydrogen-rich gas compressor 34, a hydrogen separation waste gas fan 43, and a hydrogen purification separator 35.

[0067] The lower outlet of the steam preheater 27 is connected to the upper inlet of the hydrogen-rich gas waste heat boiler 28. The upper part of the steam preheater 27 is provided with a steam inlet. The lower outlet of the hydrogen-rich gas waste heat boiler 28 is connected to the upper side of the hydrogen-rich gas primary cyclone separator 29. The upper end of the hydrogen-rich gas primary cyclone separator 29 is connected to the upper side of the hydrogen-rich gas secondary cyclone separator 30. The upper end of the hydrogen-rich gas secondary cyclone separator 30 is connected to the upper side of the hydrogen-rich gas tertiary cyclone separator 31. The upper end of the hydrogen-rich gas bag filter 31 is connected to the upper side of the hydrogen purification separator 35 through a pipe with a hydrogen separation waste gas fan 43. The lower side of the hydrogen purification separator 35 is provided with a hydrogen outlet.

[0068] The upper end of the hydrogen purification separator 35 is connected to the upper side of the steam preheater 27 and the first inlet of the riser supplement burner 41 in the calcium carbonate heating and decomposition and calcium oxide carbon dioxide absorption circulation system in the oil sand through a pipe with a hydrogen separation residual gas fan 43.

[0069] The heating and decomposition system for calcium carbonate in oil sands and the circulation system for calcium oxide to absorb carbon dioxide include a riser pipe 8, a high-temperature heat carrier storage tank 13, a heat carrier cyclone separator 14, and a riser pipe supplementary burner 41.

[0070] The lower end of the riser pipe 8 is connected to the outlet end of the riser pipe supplementary burner 41, the lower outlet end of the oil sand pyrolysis reactor 6 in the oil sand and heat carrier mixed pyrolysis oil and gas production system, the lower outlet end of the oil and gas reforming reactor 7 in the oil and gas steam reforming system for absorbing carbon dioxide to generate hydrogen-rich gas, and the side outlet end of the air preheater 16 in the flue gas energy recovery and dust removal system. The upper end of the riser pipe 8 is connected to the upper end of the heat carrier cyclone separator 14. The lower end of the heat carrier cyclone separator 14 is connected to the upper end of the high-temperature heat carrier storage tank 13. The upper end of the heat carrier cyclone separator 14 is connected to the upper end of the air preheater 16 in the flue gas energy recovery and dust removal system. The lower end of the riser pipe 8 is provided with a discharge outlet for cement admixture calcium slag.

[0071] The flue gas energy recovery and dust removal system includes an air preheater 16, a flue gas waste heat boiler 17, a primary flue gas cyclone separator 18, a secondary flue gas cyclone separator 19, a flue gas bag filter 20, and a flue gas exhaust fan 21.

[0072] The air preheater 16 is provided with an air inlet at its upper part. The lower end of the air preheater 16 is connected to the upper end of the flue gas waste heat boiler 17. The lower end of the flue gas waste heat boiler 17 is connected to the upper side of the primary flue gas cyclone separator 18. The upper end of the primary flue gas cyclone separator 18 is connected to the upper side of the secondary flue gas cyclone separator 19. The upper end of the secondary flue gas cyclone separator 19 is connected to the upper side of the flue gas bag filter 20. The upper end of the flue gas bag filter 20 is connected to the flue gas exhaust fan 21.

[0073] The cement admixture collection system includes a cement admixture calcium oxide collector 24 and a cement admixture calcium carbonate collector 32.

[0074] The upper end of the cement admixture calcium oxide collector 24 is connected to the lower end of the primary flue gas cyclone separator 18, the secondary flue gas cyclone separator 19, and the flue gas bag filter 20 in the flue gas energy recovery dust removal system. The lower end of the cement admixture calcium oxide collector 24 is provided with an outlet for the mud admixture calcium oxide powder 23.

[0075] The upper end of the cement admixture calcium carbonate collector 32 is connected to the lower end of the hydrogen-rich gas primary cyclone separator 29, the hydrogen-rich gas secondary cyclone separator 30, and the hydrogen-rich gas bag filter 31 in the hydrogen-rich gas heat recovery dust removal and purification hydrogen production system. The lower end of the cement admixture calcium carbonate collector 32 is provided with a cement admixture calcium carbonate powder 33 discharge port.

[0076] The operation process of the high-oil-content and high-calcium-content oil sand hydrogen production and cement admixture co-production process is as follows:

[0077] The raw material oil sand 1 is processed by oil sand crusher 2 to a particle size range of 0-10mm and then sent to oil sand storage tank 3 for later use. The oil sand enters mixer 5 via oil sand sealed conveyor belt 4, where it mixes with heat carrier from high-temperature (800-850℃) heat carrier storage tank 13 to initiate a pyrolysis reaction. The temperature is controlled at 450-500℃. The generated oil vapor and oil sand semi-coke (the residual solids after oil sand pyrolysis, containing residual carbon) enter oil sand pyrolysis reactor 6 to complete the pyrolysis reaction. Oil sand pyrolysis reactor 6 uses a moving bed, with materials flowing from top to bottom. The temperature is controlled at 450-500℃. The generated oil vapor enters oil gas reforming reactor 7, and oil sand semi-coke and heat carrier enter together... The material enters the riser 8; inside the riser 8, the residual carbon in the semi-coke of the oil sands and the residual carbon adsorbed on the heat carriers from the oil and gas reforming reactor 7 and the oil sands pyrolysis reactor 6 are burned, providing energy for the decomposition of calcium carbonate into calcium oxide and carbon dioxide. At the same time, the riser supplements the energy of the burner 41. The riser 8 adopts the form of an airflow bed, with the material flowing from bottom to top, and the temperature is controlled at 800-850℃. Inside the riser 8, the calcium oxide obtained from the decomposition of calcium carbonate (calcium oxide is both a catalyst for the next step of the oil and gas reforming reaction and an absorbent for carbon dioxide) is produced.

[0078] The oil sands pyrolysis reactor 6 is connected to the oil and gas reforming reactor 7 via an insulated pipe. The oil and gas produced by the oil sands pyrolysis reactor 6 enters the oil and gas reforming reactor 7 and undergoes a reforming reaction with water vapor to produce hydrogen and carbon monoxide. The oil and gas reforming reactor 7 adopts a fluidized bed form and controls the temperature at 650-700℃. At the same time, a water-gas shift reaction and a reaction in which calcium oxide absorbs carbon dioxide to produce calcium carbonate occur, making the water-gas shift reaction proceed in a direction that is more conducive to the production of hydrogen. Meanwhile, the calcium carbonate produced enters the riser pipe 8, burns until it is covered with carbon residue, and decomposes into calcium oxide and carbon dioxide at a high temperature (800-850℃). After passing through the riser and the heat carrier cyclone separator 14, it enters the high-temperature heat carrier storage tank 13 to start a new reaction regeneration cycle.

[0079] The oil and gas reforming reactor 7 is connected to the calcium carbonate powder cyclone separator 25 via an insulated pipe. The calcium carbonate powder carried out by the hydrogen-rich gas of the reaction product, including unreacted calcium oxide powder, is recovered and circulated through the calcium carbonate powder circulation control U valve 26 to maintain the stability of the fluidized bed in the oil and gas reforming reactor 7. At the same time, cement admixture products are collected by the hydrogen-rich gas primary cyclone separator 29, the hydrogen-rich gas secondary cyclone separator 30, and the hydrogen-rich gas bag filter 31.

[0080] The hydrogen-rich gas produced by the high-temperature (650-700℃) reaction is processed by a steam preheater 27 and a hydrogen-rich gas waste heat boiler 28 for waste heat utilization. It then undergoes dust removal via a primary hydrogen-rich gas cyclone separator 29, a secondary hydrogen-rich gas cyclone separator 30, and a hydrogen-rich gas bag filter 31. After being pressurized by a hydrogen-rich gas compressor 34, it enters a hydrogen purification separator 35 to obtain the final product. The hydrogen purification separator 35 uses membrane separation to control the hydrogen concentration of the product to be greater than 99%. The residual gas (methane, carbon monoxide, and carbon dioxide) separated by the hydrogen purification separator 35 is pressurized by a hydrogen separation residual gas fan 43. Part of this gas is used to supplement the burner 41 in the riser pipe, releasing heat to replenish the energy of the riser pipe 8. The other part is used for heat exchange in the steam preheater 27 to supplement the fluidizing gas in the oil and gas reforming reactor 7.

[0081] The flue gas generated from combustion in riser 8 is separated into heat carriers by heat carrier cyclone separator 14 and enters air preheater 16 and flue gas waste heat boiler 17 to recover heat. After passing through primary flue gas cyclone separator 18, secondary flue gas cyclone separator 19 and flue gas bag filter 20, calcium oxide powder is collected as a cement admixture product. At the same time, the flue gas is discharged by flue gas exhaust fan 21. The air preheated by air preheater 16 (temperature 450℃) is partly used as combustion aid 40 in riser supplementary burner 41 and partly enters riser 8 as combustion aid for residual carbon. The bottom of riser 8 collects and discharges heat carrier particles that cannot be lifted (cement admixture calcium slag 42, including calcium carbonate particles and calcium oxide particles) as a cement admixture product.

[0082] The above description is merely a few embodiments of this application and is not intended to limit this application in any way. Although this application discloses preferred embodiments as described above, it is not intended to limit this application. Any changes or modifications made by those skilled in the art without departing from the scope of the technical solution of this application using the disclosed technical content are equivalent to equivalent implementation cases and fall within the scope of the technical solution.

Claims

1. A process flow structure for the co-production of cement admixtures from high-oil-content and high-calcium-content oil sands for hydrogen production, characterized in that, The process flow structure for producing hydrogen from high-oil and high-calcium oil sands and co-producing cement admixtures consists of an oil sands and heat carrier mixing and pyrolysis system for producing oil and gas, an oil and gas steam reforming system for absorbing carbon dioxide to generate hydrogen-rich gas, a hydrogen-rich gas heat recovery, dust removal and purification system, a calcium carbonate in oil sands heating and decomposition system and a calcium oxide carbon dioxide absorption circulation system, a flue gas energy recovery and dust removal system, and a cement admixture collection system.

2. The process flow structure for hydrogen production and cement admixture co-production from high-oil-content and high-calcium-content oil sands according to claim 1, characterized in that, The inlet of the oil sand crusher (2) is connected to the input pipeline of the raw material oil sand (1), the outlet of the oil sand crusher (2) is connected to the inlet of the oil sand storage tank (3), the outlet of the oil sand storage tank (3) is located at the feed end of the oil sand sealing conveyor belt (4), the discharge end of the conveyor belt (4) is located at the first inlet of the mixer (5), and the outlet of the mixer (5) is connected to the inlet of the oil sand pyrolysis reactor (6). The upper outlet of the oil sand pyrolysis reactor (6) is connected to the lower part of the oil and gas reforming reactor (7) in the oil and gas steam reforming system for absorbing carbon dioxide and generating hydrogen-rich gas. The second inlet of the mixer (5) is connected to the first outlet of the high-temperature heat carrier storage tank (13) in the oil sand heating and decomposition system for calcium carbonate and calcium oxide absorption of carbon dioxide.

3. The process flow structure for hydrogen production and cement admixture co-production from high-oil-content and high-calcium-content oil sands according to claim 2, characterized in that, The upper part of the oil and gas reforming reactor (7) is connected to the inlet of the calcium carbonate powder cyclone separator (25) through an insulated pipe. The lower outlet of the calcium carbonate powder cyclone separator (25) is connected to the lower part of the oil and gas reforming reactor (7) through an insulated pipe equipped with a calcium carbonate powder circulation control U valve (26). The secondary feed switch valve (12) and the secondary feed control U valve (10) of calcium oxide powder are sequentially installed on the secondary feed pipe in the upper part of the oil and gas reforming reactor (7). The primary feed switch valve (11) and the primary feed control U valve (9) of calcium oxide powder are sequentially installed on the primary feed pipe in the lower part of the oil and gas reforming reactor (7). The oil and gas reforming reactor (7) is connected to the second outlet of the high-temperature heat carrier storage tank (13) in the calcium carbonate heating and decomposition and calcium oxide carbon dioxide absorption circulation system in the oil sands through a primary feed pipe and a secondary feed pipe. The upper outlet of the calcium carbonate powder cyclone separator (25) is connected to the upper inlet of the steam preheater (27) in the hydrogen-rich gas heat recovery, dust removal and purification hydrogen production system.

4. The process flow structure for hydrogen production and cement admixture co-production from high-oil-content and high-calcium-content oil sands according to claim 3, characterized in that, The lower outlet of the steam preheater (27) is connected to the upper inlet of the hydrogen-rich gas waste heat boiler (28). The upper part of the steam preheater (27) is provided with a steam inlet. The lower outlet of the hydrogen-rich gas waste heat boiler (28) is connected to the upper side of the hydrogen-rich gas primary cyclone separator (29). The upper end of the hydrogen-rich gas primary cyclone separator (29) is connected to the upper side of the hydrogen-rich gas secondary cyclone separator (30). The upper end of the hydrogen-rich gas secondary cyclone separator (30) is connected to the upper side of the hydrogen-rich gas bag filter (31). The upper end of the hydrogen-rich gas bag filter (31) is connected to the upper side of the hydrogen purification separator (35) through a pipe with a hydrogen-rich gas compressor (34). The lower side of the hydrogen purification separator (35) is provided with a hydrogen outlet. The upper end of the hydrogen purification separator (35) is connected to the upper side of the steam preheater (27) and the first inlet of the riser supplement burner (41) in the calcium carbonate heating and decomposition and calcium oxide carbon dioxide absorption circulation system in the oil sand through a pipe with a hydrogen-rich gas compressor (34).

5. The process flow structure for hydrogen production and cement admixture co-production from high-oil-content and high-calcium-content oil sands according to claim 4, characterized in that, The lower end of the riser (8) is connected to the outlet of the riser supplementary burner (41), the lower outlet of the oil sand pyrolysis reactor (6) in the oil sand and heat carrier mixed pyrolysis oil and gas production system, the lower outlet of the oil and gas reforming reactor (7) in the oil and gas steam reforming system for absorbing carbon dioxide to generate hydrogen-rich gas, and the side outlet of the air preheater (16) in the flue gas energy recovery and dust removal system. The upper end of the riser (8) is connected to the upper end of the heat carrier cyclone separator (14). The lower end of the heat carrier cyclone separator (14) is connected to the upper end of the high temperature heat carrier storage tank (13). The upper end of the heat carrier cyclone separator (14) is connected to the upper end of the air preheater (16) in the flue gas energy recovery and dust removal system. The lower end of the riser (8) is provided with a discharge port for cement admixture calcium slag.

6. The process flow structure for hydrogen production and cement admixture co-production from high-oil-content and high-calcium-content oil sands according to claim 5, characterized in that, An air inlet is provided at the upper part of the air preheater (16). The lower end of the air preheater (16) is connected to the upper end of the flue gas waste heat boiler (17). The lower end of the flue gas waste heat boiler (17) is connected to the upper side of the first-stage flue gas cyclone separator (18). The upper end of the first-stage flue gas cyclone separator (18) is connected to the upper side of the second-stage flue gas cyclone separator (19). The upper end of the second-stage flue gas cyclone separator (19) is connected to the upper side of the flue gas bag filter (20). The upper end of the flue gas bag filter (20) is connected to the flue gas exhaust fan (21).

7. The process flow structure for hydrogen production and cement admixture co-production from high-oil-content and high-calcium-content oil sands according to claim 1, characterized in that, The upper end of the cement admixture calcium oxide collector (24) is connected to the lower end of the primary flue gas cyclone separator (18), the secondary flue gas cyclone separator (19), and the flue gas bag filter (20) in the flue gas energy recovery dust removal system, respectively. The lower end of the cement admixture calcium oxide collector (24) is provided with an outlet for mud admixture calcium oxide powder (23). The upper end of the cement admixture calcium carbonate collector (32) is connected to the lower end of the hydrogen-rich gas primary cyclone separator (29), the hydrogen-rich gas secondary cyclone separator (30), and the hydrogen-rich gas bag filter (31) in the hydrogen-rich gas heat recovery dust removal and purification hydrogen production system. The lower end of the cement admixture calcium carbonate collector (32) is provided with a cement admixture calcium carbonate powder (33) outlet.

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