Chemical-looping ammonia production system taking high-sulfur petroleum coke and coal as raw materials

Abstract

The invention discloses a chemical-looping ammonia production system taking high-sulfur petroleum coke and coal as raw materials. The chemical-looping ammonia production system comprises a chemical-looping hydrogen production unit, an air reactor waste heat power generation unit, a steam reactor waste heat power generation unit, a fuel reactor waste heat power generation unit and a synthesis ammonia unit. Compared with a high-sulfur petroleum coke gasification ammonia production system, the system provided by the invention has the advantages that a chemical looping hydrogen production process is used, and waste heat recovery is carried out on outlet gas of each reactor by adopting multiple waste heat recovery modes, so that a high-energy-consumption water gas change unit, an air separation unit and an acid gas removal unit in the high-sulfur petroleum coke gasification ammonia production process are omitted; and the system energy consumption is reduced.

Description

Technical Field

[0001] The invention relates to the technical field of ammonia preparation systems, and in particular to a chemical chain ammonia preparation system using high-sulfur petroleum coke and coal as raw materials. Background Art

[0002] There are several ways to store hydrogen: compressed gas storage, cryogenic liquefaction storage, solid adsorption storage, etc. Compressed hydrogen is usually stored in high-pressure gas cylinders. Compressed gas storage has safety risks caused by high storage pressure and low energy density of stored hydrogen. Cryogenic liquefaction of hydrogen can significantly increase the storage density of hydrogen. The density of liquid hydrogen can reach 70kg / m at standard atmospheric pressure. 3 . The process of using liquid hydrogen to store hydrogen has the advantages of high energy density and safety, but the energy consumption and cost of hydrogen liquefaction are high. Solid adsorption hydrogen storage uses porous materials to adsorb hydrogen, and the hydrogen storage capacity can reach 8-10wt% at a low temperature of -196 ℃, and only 1 wt% at room temperature. Ammonia can be liquefied when it is compressed to 1 MPa at 25 ℃ or cooled to -33 ℃ at normal pressure. The conditions for hydrogen storage using ammonia are milder than those for hydrogen liquefaction, and the storage and transportation costs are relatively low. Ammonia has a higher calorific value than hydrogen and can be regarded as a new generation of clean and efficient gas fuel. In addition, ammonia is also an important fertilizer and chemical raw material.

[0003] Petroleum coke is a by-product of the oil refining process, with the characteristics of high carbon content, high calorific value and low ash content. With the increase in the supply of heavy oil and the refining of inferior crude oil worldwide, the output of petroleum coke continues to increase. Petroleum coke is divided into low-sulfur and high-sulfur petroleum coke according to the sulfur content. Among them, low-sulfur petroleum coke is mainly used to produce graphite electrode materials, which has high market demand and economic value, while high-sulfur petroleum coke has a high sulfur content and is corrosive to equipment, which limits its application. It is generally used as a fuel for heating and power generation. Direct combustion of high-sulfur petroleum coke will cause serious environmental problems. Petroleum coke gasification is a more environmentally friendly method of utilizing petroleum coke.

[0004] The existing high-sulfur petroleum coke and coal co-gasification process for ammonia production is as follows: Figure 1 As shown, it includes a gasification unit 1, a water-gas conversion unit 2, an acid gas removal unit 3, CO and CO 2 Methanation unit 4, synthetic ammonia unit 5 and air separation unit 6. The air separation unit, water gas change unit and acid gas removal unit in the existing petroleum coke gasification process all consume a lot of energy, resulting in the petroleum coke and coal co-gasification ammonia production system still has problems such as low system exergy efficiency and high greenhouse gas emissions. Summary of the invention

[0005] The purpose of the present invention is to remedy the defects of the prior art and provide a chemical chain ammonia production system using high-sulfur petroleum coke and coal as raw materials.

[0006] The present invention is achieved through the following technical solutions: A chemical chain ammonia production system using high-sulfur petroleum coke and coal as raw materials, comprising a chemical chain hydrogen production unit, an air reactor waste heat power generation unit, a steam reactor waste heat power generation unit, a fuel reactor waste heat power generation unit and a synthetic ammonia unit; The chemical chaining hydrogen production unit is provided with a high-sulfur petroleum coke and coal inlet, a water vapor inlet, a water inlet, a hot air inlet, a flue gas outlet, a nitrogen-rich gas outlet, and a hydrogen and water vapor outlet. The high-sulfur petroleum coke and coal are introduced into the chemical chaining hydrogen production unit through the high-sulfur petroleum coke and coal inlets, the water vapor is introduced into the chemical chaining hydrogen production unit through the water vapor inlet, the water is introduced into the chemical chaining hydrogen production unit through the water inlet, and the hot air is introduced into the chemical chaining hydrogen production unit through the hot air inlet. The high-sulfur petroleum coke and coal, the water vapor, the water, and the hot air pass through the chemical chaining hydrogen production unit to obtain flue gas, nitrogen-rich gas, hydrogen, and water vapor. The air reactor waste heat power generation unit is provided with a nitrogen-rich gas inlet, a water inlet, an air inlet, an air outlet and a nitrogen-rich gas outlet. The nitrogen-rich gas outlet of the chemical chain hydrogen production unit is connected to the nitrogen-rich gas inlet of the air reactor waste heat power generation unit through a pipeline. The nitrogen-rich gas is introduced into the air reactor waste heat power generation unit through the nitrogen-rich gas inlet, the water is introduced into the air reactor waste heat power generation unit through the water inlet, and the air is introduced into the air reactor waste heat power generation unit through the air inlet. The nitrogen-rich gas is firstly generated by a gas turbine, and then heat-exchanged with water to obtain high-pressure steam. The high-pressure steam is generated by a steam turbine, and the nitrogen-rich gas after heat-exchange with water is preheated to the air. The air outlet of the air reactor waste heat power generation unit is connected to the air inlet of the chemical chain hydrogen production unit, and the preheated air is introduced into the chemical chain hydrogen production unit; the nitrogen-rich gas outlet of the air reactor waste heat power generation unit is connected to the nitrogen-rich gas inlet of the synthetic ammonia unit, and the nitrogen-rich gas is transported to the synthetic ammonia unit through a pipeline; The steam reactor waste heat power generation unit is provided with a water inlet, a hydrogen and water vapor inlet, a water vapor outlet and a hydrogen outlet. The hydrogen and water vapor outlet of the chemical chain hydrogen production unit is connected to the hydrogen and water vapor inlet of the steam reactor waste heat power generation unit through a pipeline. Water is introduced into the steam reactor waste heat power generation unit through the water inlet. Hydrogen and water vapor are introduced into the steam reactor waste heat power generation unit through the hydrogen and water vapor inlet. Hydrogen and water vapor are heat-exchanged with water to obtain high-pressure steam. The high-pressure steam is generated by a steam turbine. The cooled hydrogen and water vapor are heat-exchanged with water to obtain water vapor. The water vapor outlet of the steam reactor waste heat power generation unit is connected to the water vapor inlet of the chemical chain hydrogen production unit. The water vapor is introduced into the chemical chain hydrogen production unit through a pipeline. The hydrogen outlet of the steam reactor waste heat power generation unit is connected to the hydrogen inlet of the synthetic ammonia unit. The hydrogen is transported to the synthetic ammonia unit through a pipeline. The fuel reactor waste heat power generation unit is provided with a flue gas inlet, a water inlet and a CO 2The flue gas outlet of the chemical chain hydrogen production unit is connected to the flue gas inlet of the fuel reactor waste heat power generation unit through a pipeline, the flue gas is introduced into the fuel reactor waste heat power generation unit through the flue gas inlet, and water is introduced into the fuel reactor waste heat power generation unit through the water inlet. The flue gas first passes through a gas turbine to generate electricity, and then exchanges heat with water to obtain high-pressure steam. The high-pressure steam generates electricity through a steam turbine, and the cooled flue gas is separated and dehydrated by flash evaporation to obtain high-purity CO 2 , and finally compressed to obtain high-pressure carbon dioxide, which is then passed through a pipeline from CO 2 Export output; The synthetic ammonia unit is provided with a nitrogen-rich gas inlet, a hydrogen inlet, a purge gas outlet and a liquid ammonia outlet. The hydrogen at the outlet of the steam reactor waste heat power generation unit and the nitrogen-rich gas in the air reactor waste heat power generation unit are respectively introduced into the synthetic ammonia unit through the hydrogen inlet and the nitrogen-rich gas inlet. The synthetic ammonia unit generates electricity and obtains purge gas and liquid ammonia, which are respectively output from the purge gas outlet and the liquid ammonia outlet.

[0007] The chemical chain hydrogen production unit comprises a steam reactor, an air reactor, a fuel reactor, a first pump and a flow divider; The first pump is provided with a water inlet and a water outlet, and the first pump pressurizes the water, and the pressurized water is delivered to the fuel reactor; The fuel reactor is provided with a high-sulfur petroleum coke and coal inlet, a water inlet, an oxygen carrier inlet, a flue gas outlet and a reduced oxygen carrier outlet. The water at the first water pump outlet is introduced into the fuel reactor through the water inlet, the oxygen carrier coming out of the air reactor is introduced into the fuel reactor through the oxygen carrier inlet, and the high-sulfur petroleum coke and coal are introduced into the fuel reactor through the high-sulfur petroleum coke and coal inlets. In the fuel reactor, the high-sulfur petroleum coke and coal, water and the oxygen carrier react to generate high-temperature flue gas and reduced oxygen carrier. The splitter is provided with a reducing oxygen carrier inlet and a reducing oxygen carrier outlet, and the reducing oxygen carrier outlet of the fuel reactor is connected to the reducing oxygen carrier inlet of the splitter through a pipeline; the reducing oxygen carrier at the reducing oxygen carrier outlet of the fuel reactor is divided into a first reducing oxygen carrier and a second reducing oxygen carrier in the splitter; The steam reactor is provided with a reducing oxygen carrier inlet, a water vapor inlet, a partially oxidized reducing oxygen carrier outlet and a hydrogen and water vapor outlet. The first reducing oxygen carrier of the diverter is introduced into the steam reactor through the reducing oxygen carrier inlet, and the water vapor at the water vapor outlet of the waste heat power generation unit of the steam reactor is introduced into the steam reactor. The first reducing oxygen carrier undergoes a partial oxidation reaction with the water vapor in the steam reactor to generate hydrogen and water vapor as well as the partially oxidized reducing oxygen carrier. The air reactor is provided with a partially oxidized reducing oxygen carrier inlet, a reducing oxygen carrier inlet, a hot air inlet, an oxygen carrier outlet and a nitrogen-rich gas outlet. The partially oxidized reducing oxygen carrier outlet of the steam reactor is connected to the partially oxidized reducing oxygen carrier inlet of the air reactor through a pipeline. The partially oxidized reducing oxygen carrier is introduced into the air reactor through the partially oxidized reducing oxygen carrier inlet. The second reducing oxygen carrier at the epoxy oxygen carrier outlet of the splitter is introduced into the air reactor through the reducing oxygen carrier inlet. The hot air at the hot air outlet of the waste heat power generation unit of the air reactor is introduced into the air reactor through the hot air inlet. The oxygen in the hot air oxidizes the second reducing oxygen carrier and the partially oxidized reducing oxygen carrier into oxygen carriers, and the oxygen carriers are transported to the fuel reactor through a pipeline. The hot air consumes the oxygen to obtain nitrogen-rich gas, and the nitrogen-rich gas is input into the waste heat power generation unit of the air reactor through the nitrogen-rich gas outlet.

[0008] The fuel reactor waste heat power generation unit includes a first gas turbine, a second pump, a first heat exchanger, a first steam turbine unit, a first flash tank and a first multi-stage compressor; The first gas turbine is provided with a flue gas inlet and a flue gas outlet, the high-temperature flue gas at the flue gas outlet of the fuel reactor is introduced into the gas turbine to generate electricity, and the remaining high-temperature flue gas is output from the flue gas outlet; The second pump is provided with a water inlet and a water outlet, and the second pump pressurizes the water, and the pressurized water is transported to the first heat exchanger; The first heat exchanger is provided with a flue gas inlet, a water inlet, a flue gas outlet and a water vapor outlet. The water pressurized by the second pump is introduced into the first heat exchanger through the water inlet. The high-temperature flue gas at the flue gas outlet of the first gas turbine is introduced into the first heat exchanger through the flue gas inlet. In the first heat exchanger, the high-temperature flue gas exchanges heat with water to generate high-pressure steam. The first steam turbine unit is provided with a high-pressure steam inlet. The high-pressure steam is introduced into the first steam turbine unit from the high-pressure steam inlet to perform work and generate electricity. The remaining flue gas in the first heat exchanger is output from the flue gas outlet. The first flash tank is provided with a flue gas inlet, a CO 2 The remaining flue gas in the first heat exchanger is input into the first flash tank from the flue gas inlet. The flue gas is flashed through the first flash tank and the liquid is separated to obtain CO 2 mixture of gas and liquid phase; The first multi-stage compressor is provided with a CO 2 Inlet and CO 2 Export, first flash tank CO 2 CO at gas outlet 2 The gas is passed into the first multi-stage compressor for pressurization. 2 From CO 2 Export output.

[0009] The steam reactor waste heat power generation unit comprises a third pump, a second heat exchanger, a desulfurization device, a second steam turbine unit, a fourth pump, a third heat exchanger and a second flash tank; The third pump is provided with a water inlet and a water outlet, and the third pump pressurizes water, and the pressurized water is transported to the second heat exchanger; The second heat exchanger is provided with a hydrogen and water vapor inlet, a water inlet, a hydrogen and water vapor outlet and a high-pressure steam outlet. Water from the third pump is introduced into the second heat exchanger through the water inlet. The hydrogen and water vapor outputted from the hydrogen and water vapor outlet of the steam reactor are introduced into the second heat exchanger. The hydrogen and water vapor exchange heat with water in the second heat exchanger to generate high-pressure steam and hydrogen and water vapor. The second steam turbine unit is provided with a high-pressure steam inlet. The high-pressure steam is introduced into the second steam turbine unit to generate electricity by performing work. The desulfurization device is provided with a hydrogen and water vapor inlet and a hydrogen and water vapor outlet. The hydrogen and water vapor outlet of the second heat exchanger is connected to the hydrogen and water vapor inlet of the desulfurization device through a pipeline, and hydrogen and water vapor are introduced into the desulfurization device for desulfurization treatment. The desulfurization device is a Fe-containing 2 O 3 Desulfurization device with ZnO bed.

[0010] The fourth pump is provided with a water inlet and a water outlet, and the fourth pump pressurizes the water, and the pressurized water is transported to the third heat exchanger; The third heat exchanger is provided with a hydrogen and water vapor inlet, a water inlet, a hydrogen and water vapor outlet, and a water vapor outlet. The hydrogen and water vapor outlet of the desulfurization device is connected to the hydrogen and water vapor inlet of the third heat exchanger through a pipeline. Hydrogen and water vapor exchange heat with water to generate water vapor and hydrogen and water vapor. The water vapor is introduced into the steam reactor through the water vapor outlet. The second flash tank is provided with a hydrogen and water vapor inlet, a hydrogen outlet and a water outlet. The hydrogen and water vapor outlet of the third heat exchanger is connected to the hydrogen and water vapor inlet of the second flash tank through a pipeline. The hydrogen and water vapor are separated by flash evaporation to obtain hydrogen and water.

[0011] The air reactor waste heat power generation unit comprises a second multi-stage compressor, a fourth heat exchanger, a fifth heat exchanger, a second gas turbine, a fifth pump and a third steam turbine unit; The second gas turbine is provided with a nitrogen-rich gas inlet and a nitrogen-rich gas outlet. The nitrogen-rich gas at the nitrogen-rich gas outlet of the air reactor is introduced into the second gas turbine to generate electricity, and the remaining nitrogen-rich gas is output from the nitrogen-rich gas outlet. The fifth pump is provided with a water inlet and a water outlet, and the fifth pump pressurizes the water, and the pressurized water is input into the fourth heat exchanger; The fourth heat exchanger is provided with a nitrogen-rich gas inlet, a water inlet, a nitrogen-rich gas outlet and a high-pressure steam outlet. The nitrogen-rich gas outlet of the second gas turbine is connected to the nitrogen-rich gas inlet of the fourth heat exchanger through a pipeline, and the nitrogen-rich gas exchanges heat with water to obtain high-pressure steam; the third steam turbine unit is provided with a high-pressure steam inlet, and the high-pressure steam is introduced into the third steam turbine unit, and the high-pressure steam performs work in the third steam turbine unit to generate electricity; The second multi-stage compressor is provided with an air inlet and an air outlet, and the air is pressurized by the second multi-stage compressor and output to the fifth heat exchanger; The fifth heat exchanger is provided with an air inlet, a nitrogen-rich gas inlet, a hot air outlet and a nitrogen-rich gas outlet. The nitrogen-rich gas outlet of the fourth heat exchanger is connected to the nitrogen-rich gas inlet of the fifth heat exchanger through a pipeline. The air outlet of the second multi-stage compressor is connected to the air inlet of the fifth heat exchanger through a pipeline. The nitrogen-rich gas preheats the air in the fifth heat exchanger, and the nitrogen-rich gas after heat exchange is output from the nitrogen-rich gas outlet. The hot air is transported to the air reactor through the hot air outlet.

[0012] The synthetic ammonia unit comprises a third multi-stage compressor, a fourth multi-stage compressor, a first gas mixer, a deoxygenation reactor, a third flash tank, a first gas splitter, a second gas mixer, a sixth heat exchanger, a first synthetic ammonia reactor, a third gas mixer, a second synthetic ammonia reactor, a fourth gas mixer, a third synthetic ammonia reactor, a seventh heat exchanger, a second gas splitter, a compressor, an organic Rankine cycle device, a cooler, a fourth flash tank, and a fifth flash tank; The third multi-stage compressor is provided with a hydrogen inlet and a hydrogen outlet, the hydrogen at the hydrogen outlet of the steam reactor waste heat power generation unit is compressed in the first compressor, and the compressed hydrogen is output through the hydrogen outlet; The fourth multi-stage compressor is provided with a nitrogen-rich gas inlet and a nitrogen-rich gas outlet, the nitrogen-rich gas outputted from the nitrogen-rich gas outlet of the fifth heat exchanger is compressed in the fourth multi-stage compressor, and the compressed nitrogen-rich gas is outputted through the nitrogen-rich gas outlet; The first gas mixer is provided with a nitrogen-rich gas inlet, a hydrogen inlet and a fresh synthesis gas outlet. The hydrogen at the hydrogen outlet of the third multi-stage compressor and the nitrogen-rich gas at the nitrogen-rich outlet of the second compressor are respectively transported to the first gas mixer through the hydrogen inlet and the nitrogen-rich inlet, mixed into fresh synthetic ammonia raw gas, and output from the fresh synthesis gas outlet. The deoxygenation reactor is provided with a fresh synthetic ammonia raw gas inlet and a fresh synthetic ammonia raw gas outlet. The fresh synthetic ammonia raw gas at the fresh synthetic gas outlet of the first gas mixer is input into the deoxygenation reactor from the fresh synthetic ammonia raw gas inlet. The fresh synthetic ammonia raw gas is deoxygenated in the deoxygenation reactor and then output into the third flash tank from the fresh synthetic ammonia raw gas outlet. The third flash tank is provided with a fresh synthetic ammonia raw gas inlet, a fresh synthetic ammonia raw gas outlet and a water outlet. The fresh synthetic ammonia raw gas of the deoxygenation reactor is introduced into the third flash tank from the fresh synthetic ammonia raw gas inlet. The fresh synthetic ammonia raw gas is flashed to separate water and output from the water outlet. The fresh synthetic ammonia raw gas after water separation is output through the fresh synthetic ammonia raw gas outlet. The second gas mixer is provided with a fresh synthetic ammonia raw gas inlet, an unreacted gas inlet and a synthetic ammonia raw gas outlet. The fresh synthetic ammonia raw gas at the fresh synthetic ammonia raw gas outlet of the third flash tank is input into the second gas mixer through the fresh synthetic ammonia raw gas inlet, and the unreacted gas at the compressor outlet is introduced into the second gas mixer through the unreacted gas inlet. The fresh synthetic ammonia raw gas and the unreacted gas are mixed into the synthetic ammonia raw gas and output through the synthetic ammonia raw gas outlet. The first gas splitter is provided with a synthetic ammonia raw gas inlet, a first synthetic ammonia raw gas outlet, a second synthetic ammonia raw gas outlet and a third synthetic ammonia raw gas outlet. The synthetic ammonia raw gas at the synthetic ammonia raw gas outlet of the second gas mixer is input into the first gas splitter through the synthetic ammonia raw gas inlet. In the first gas splitter, the synthetic ammonia raw gas is split into three synthetic ammonia raw gases, namely the first synthetic ammonia raw gas, the second synthetic ammonia raw gas and the third synthetic ammonia raw gas. The sixth heat exchanger is provided with a high-temperature mixed gas inlet, a first synthetic ammonia raw gas inlet, a high-temperature mixed gas outlet and a first synthetic ammonia raw gas outlet. The first synthetic ammonia raw gas of the first gas splitter is introduced into the sixth heat exchanger through the first synthetic ammonia raw gas inlet. The high-temperature mixed gas outputted from the third synthetic ammonia reactor is introduced into the sixth heat exchanger through the high-temperature mixed gas inlet of the sixth heat exchanger. In the sixth heat exchanger, the high-temperature mixed gas preheats the first synthetic ammonia raw gas. The first ammonia synthesis reactor is provided with an ammonia synthesis raw gas inlet and a high-temperature mixed gas outlet. The first ammonia synthesis raw gas at the first ammonia synthesis raw gas outlet of the sixth heat exchanger is introduced into the ammonia synthesis reactor through the ammonia synthesis raw gas inlet of the first ammonia synthesis reactor. The first ammonia synthesis raw gas generates a high-temperature mixed gas in the first ammonia synthesis reactor, and the high-temperature mixed gas is output from the high-temperature mixed gas outlet. The third gas mixer is provided with a second synthetic ammonia raw gas inlet, a high-temperature mixed gas inlet and a synthetic ammonia mixed gas outlet. The high-temperature mixed gas output from the first synthetic ammonia reactor is input into the third gas mixer from the high-temperature mixed gas inlet. The second synthetic ammonia raw gas output from the first gas splitter is transported into the third gas mixer through the second synthetic ammonia raw gas inlet to be mixed into a synthetic ammonia mixed gas. The synthetic ammonia mixed gas is output from the synthetic ammonia mixed gas outlet. The second ammonia synthesis reactor is provided with an ammonia mixture inlet and a high-temperature mixed gas outlet. The ammonia mixture at the ammonia mixture outlet of the third gas mixer is input into the second ammonia synthesis reactor through the ammonia mixture inlet. The ammonia mixture reacts in the second ammonia synthesis reactor to generate a high-temperature mixed gas, and the high-temperature mixed gas is output through the high-temperature mixed gas outlet. The fourth gas mixer is provided with a third synthetic ammonia raw gas inlet, a high-temperature mixed gas inlet and a synthetic ammonia mixed gas outlet. The high-temperature mixed gas output from the second synthetic ammonia reactor and the third synthetic ammonia raw gas output from the first gas splitter are respectively introduced into the fourth gas mixer through the high-temperature mixed gas inlet and the third synthetic ammonia raw gas inlet, and are mixed into a synthetic ammonia mixed gas and output through the synthetic ammonia mixed gas outlet. The third synthetic ammonia reactor is provided with a synthetic ammonia mixed gas inlet and a high-temperature mixed gas outlet. The synthetic ammonia mixed gas outputted from the fourth gas mixer is introduced into the third synthetic ammonia reactor. In the third synthetic ammonia reactor, the synthetic ammonia mixed gas reacts to generate a high-temperature mixed gas which is outputted through the high-temperature mixed gas outlet and introduced into the sixth heat exchanger through the high-temperature mixed gas inlet of the sixth heat exchanger. The seventh heat exchanger is provided with a high-temperature mixed gas inlet, an unreacted gas inlet, a high-temperature mixed gas outlet and an unreacted gas outlet. The high-temperature mixed gas outputted from the high-temperature mixer outlet of the sixth heat exchanger is introduced into the seventh heat exchanger through the high-temperature mixed gas inlet of the seventh heat exchanger. The unreacted gas outputted from the second flash tank is introduced into the seventh heat exchanger through the unreacted gas inlet. The high-temperature mixed gas and the unreacted gas exchange heat in the seventh heat exchanger. The high-temperature mixed gas preheats the unreacted gas. The high-temperature mixed gas and the unreacted gas outputted from the high-temperature mixed gas outlet and the unreacted gas outlet are introduced into the organic Rankine cycle device and the second gas splitter respectively. The second gas splitter is provided with an unreacted gas inlet, a purge gas outlet and an unreacted gas outlet, the unreacted gas outputted by the seventh heat exchanger is outputted from the purge gas outlet as purge gas at the discharge portion of the second gas splitter, and the remaining unreacted gas is outputted from the unreacted gas outlet and inputted into the compressor; The compressor is provided with an unreacted gas inlet and an unreacted gas outlet, the unreacted gas outputted by the second gas splitter is compressed by the compressor, and the pressurized unreacted gas is mixed with the fresh synthetic ammonia raw gas in the second gas mixer; The organic Rankine cycle device includes a turbine, a condenser, a sixth pump and an eighth heat exchanger. The sixth pump is provided with a low-pressure refrigerant inlet and a high-pressure refrigerant outlet. The eighth heat exchanger is provided with a high-temperature mixed gas inlet, a high-pressure refrigerant inlet, a mixed gas outlet and a high-pressure refrigerant outlet. The turbine is provided with a high-pressure refrigerant inlet and a low-pressure refrigerant outlet. The condenser is provided with a low-pressure refrigerant inlet and a low-pressure refrigerant outlet. The low-pressure refrigerant is introduced into the sixth pump, pressurized by the sixth pump to obtain a high-pressure refrigerant, which is output through the high-pressure refrigerant outlet of the sixth pump, and introduced into the eighth heat exchanger through the high-pressure refrigerant inlet of the eighth heat exchanger. The high-temperature mixed gas outputted from the eight heat exchangers is introduced through the high-temperature mixed gas inlet of the eighth heat exchanger, and after heat exchanged by the eighth heat exchanger, the mixed gas is outputted to the cooler through the mixed gas outlet of the eighth heat exchanger, and the high-pressure refrigerant is outputted through the high-pressure refrigerant outlet of the eighth heat exchanger, and is inputted into the turbine from the high-pressure refrigerant inlet of the turbine, and after power generation by the turbine, the low-pressure refrigerant is outputted through the low-pressure refrigerant outlet of the turbine, and the low-pressure refrigerant outputted from the low-pressure refrigerant outlet of the turbine is introduced into the condenser through the low-pressure refrigerant inlet of the condenser, and after being cooled by the condenser, the low-pressure refrigerant is outputted through the low-pressure refrigerant outlet of the condenser and introduced into the sixth pump; The cooler is provided with a mixed gas inlet and a mixed gas outlet. The mixed gas outputted from the mixed gas outlet of the eighth heat exchanger of the organic Rankine cycle device is passed into the cooler from the mixed gas inlet of the cooler. After the mixed gas is cooled, it is outputted through the mixed gas outlet. The fourth flash tank is provided with a mixed gas inlet, an unreacted gas outlet and a crude ammonia product outlet. The mixed gas outputted from the mixed gas outlet of the cooler is introduced into the fourth flash tank through the mixed gas inlet of the fourth flash tank. The mixed gas is separated into a crude ammonia product and unreacted gas by flash evaporation. The crude ammonia product and the unreacted gas are respectively outputted from the crude ammonia product outlet and the unreacted gas outlet. The unreacted gas is introduced into the seventh heat exchanger from the unreacted gas inlet of the seventh heat exchanger. The fifth flash tank is provided with a crude ammonia product inlet, a liquid ammonia product outlet and a tail gas outlet. The crude ammonia product output from the crude ammonia product outlet of the fourth flash tank is introduced into the crude ammonia product inlet of the fifth flash tank. The crude ammonia product is further flashed and separated in the fifth flash tank to obtain a liquid ammonia product and part of the tail gas for discharge.

[0013] The mass ratio of the coal to high sulfur petroleum coke feed is 0.8 to 1.2.

[0014] The oxygen carrier material is Fe 2 O 3 With SiC, and Fe 2 O 3 Loaded on SiC at a mass ratio of 0.7 to 1.3.

[0015] The temperature of the fuel reactor in the chemical chain hydrogen production unit is 800 ~ 1000 ° C, the pressure is 2 ~ 4 MPa, the temperature of the steam reactor is 600 ~ 800 ° C, the pressure is 2 ~ 4 MPa, and the temperature of the air fuel reactor is 1200 ~ 1400 ° C, the pressure is 2 ~ 4 MPa.

[0016] The hydrogen and rich nitrogen of the synthetic ammonia unit are mixed at a molar ratio of 2.8 to 3.2 to form fresh synthetic ammonia raw gas; the feed temperature of the synthetic ammonia reactor is 300 to 500°C and the pressure is 18 to 22 MPa.

[0017] The advantages of the present invention are as follows: compared with the high-sulfur petroleum coke gasification ammonia production system, the present invention uses a chemical chain hydrogen production process and adopts a variety of waste heat recovery methods to recover the waste heat of the outlet gas of each reactor, omitting the high-energy-consuming water gas conversion unit, air separation unit and acid gas removal unit in the high-sulfur petroleum coke gasification ammonia production process, thereby reducing the energy consumption of the system.

[0018] In the present invention, the high-sulfur petroleum coke and coal chemical chaining ammonia production system is compared with the high-sulfur petroleum coke and coal co-gasification ammonia production system. The exergy efficiency of the system is increased from 47.72% to 51.05%, and the greenhouse gas emissions of the system are increased from 1368 kg CO 2 -eq / t NH 3 Reduced to 382 kg CO 2 -eq / t NH 3 .

[0019] The present invention does not require high energy consumption unit operation in the petroleum coke gasification process, has a variety of waste heat recovery methods, and can better improve the energy efficiency of the system and reduce greenhouse gas emissions. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] Figure 1 This is the existing high-sulfur petroleum coke and coal co-gasification ammonia production flow chart; Figure 2 This is a schematic diagram of the process of the chemical chain ammonia production system of high-sulfur petroleum coke and coal of the present invention; Figure 3 It is a flow chart of the chemical chain hydrogen production unit and waste heat recovery of each reactor in the present invention.

[0021] Figure 4 This is a flow chart of the synthetic ammonia unit in the present invention. DETAILED DESCRIPTION

[0022] like Figure 2As shown, a chemical chain ammonia production system using high-sulfur petroleum coke and coal as raw materials includes a chemical chain hydrogen production unit 7, an air reactor waste heat power generation unit 8, a steam reactor waste heat power generation unit 9, a fuel reactor waste heat power generation unit 10 and a synthetic ammonia unit 5; The chemical chaining hydrogen production unit 7 is provided with a high-sulfur petroleum coke and coal inlet, a water vapor inlet, a water inlet, a hot air inlet, a flue gas outlet, a nitrogen-rich gas outlet, and a hydrogen and water vapor outlet. The high-sulfur petroleum coke and coal are introduced into the chemical chaining hydrogen production unit 7 through the high-sulfur petroleum coke and coal inlets, the water vapor is introduced into the chemical chaining hydrogen production unit 7 through the water vapor inlet, the water is introduced into the chemical chaining hydrogen production unit 7 through the water inlet, and the hot air is introduced into the chemical chaining hydrogen production unit 7 through the hot air inlet. The high-sulfur petroleum coke and coal, the water vapor, the water, and the hot air pass through the chemical chaining hydrogen production unit 7 to obtain flue gas, nitrogen-rich gas, hydrogen, and water vapor. The air reactor waste heat power generation unit 8 is provided with a nitrogen-rich gas inlet, a water inlet, an air inlet, an air outlet and a nitrogen-rich gas outlet. The nitrogen-rich gas outlet of the chemical chain hydrogen production unit 7 is connected to the nitrogen-rich gas inlet of the air reactor waste heat power generation unit 8 through a pipeline. The nitrogen-rich gas at the nitrogen-rich gas outlet of the chemical chain hydrogen production unit 7 is firstly generated by a gas turbine, and then heat-exchanged with water to obtain high-pressure steam. The high-pressure steam generates electricity through the air reactor waste heat power generation unit 8. The nitrogen-rich gas after heat-exchange with water is used to preheat the air. The preheated air is sequentially passed through the air inlet of the air reactor waste heat power generation unit 8 and the air inlet of the chemical chain hydrogen production unit 7 into the chemical chain hydrogen production unit 7; the nitrogen-rich gas at the nitrogen-rich gas outlet of the air reactor waste heat power generation unit 8 is transported to the synthetic ammonia unit 5 through a pipeline; The steam reactor waste heat power generation unit 9 is provided with a water inlet, a hydrogen and water vapor inlet, a water vapor outlet and a hydrogen outlet. The hydrogen and water vapor outlets of the chemical chain hydrogen production unit 7 are connected to the hydrogen and water vapor inlets of the steam reactor waste heat power generation unit 9 through a pipeline. The hydrogen and water vapor are heat-exchanged with water to obtain high-pressure steam, which is passed into the steam reactor waste heat power generation unit 9 to generate electricity. The cooled hydrogen and water vapor are heat-exchanged with water to obtain water vapor, which is passed into the chemical chain hydrogen production unit 7 through a pipeline; the hydrogen at the hydrogen outlet of the steam reactor waste heat power generation unit 9 is transported to the synthetic ammonia unit 5 through a pipeline; The fuel reactor waste heat power generation unit 10 is provided with a flue gas inlet, a water inlet and a CO 2 The flue gas outlet of the chemical chain hydrogen production unit 7 is connected to the flue gas inlet of the fuel reactor waste heat power generation unit 10 through a pipeline. The flue gas at the flue gas outlet of the chemical chain hydrogen production unit 7 first passes through a gas turbine to generate electricity, and then exchanges heat with water to obtain high-pressure steam. The high-pressure steam generates electricity through the fuel reactor waste heat power generation unit 10. The cooled flue gas is separated and dehydrated by flash evaporation to obtain high-purity CO 2 , and finally compressed to obtain high-pressure carbon dioxide, which is then passed through a pipeline from CO2 Export output; The synthetic ammonia unit 5 is provided with a nitrogen-rich gas inlet, a hydrogen inlet, a purge gas outlet and a liquid ammonia outlet. The hydrogen at the outlet of the steam reactor waste heat power generation unit 9 and the nitrogen-rich gas in the air reactor waste heat power generation unit 8 are respectively introduced into the synthetic ammonia unit 5 through the hydrogen inlet and the nitrogen-rich gas inlet. The synthetic ammonia unit 5 generates electricity and obtains purge gas and liquid ammonia, which are respectively output from the purge gas outlet and the liquid ammonia outlet.

[0023] like Figure 3 As shown, the chemical chain hydrogen production unit 7 includes a steam reactor 11, an air reactor 12, a fuel reactor 13, a first pump 14 and a flow divider 15; The first pump 14 is provided with a water inlet and a water outlet. The first pump 14 pressurizes the water and delivers the pressurized water to the fuel reactor 13. The fuel reactor 13 is provided with a high-sulfur petroleum coke and coal inlet, a water inlet, an oxygen carrier inlet, a flue gas outlet and a reduced oxygen carrier outlet. The water at the water outlet of the first pump 14 is introduced into the fuel reactor 13 through the water inlet. The oxygen carrier coming out of the air reactor 12 is introduced into the fuel reactor 13 through the oxygen carrier inlet. The high-sulfur petroleum coke and coal are introduced into the fuel reactor 13 through the high-sulfur petroleum coke and coal inlets. In the fuel reactor 13, the high-sulfur petroleum coke and coal, water and oxygen carrier react to generate high-temperature flue gas and reduced oxygen carrier. The splitter 15 is provided with a reducing oxygen carrier inlet and a reducing oxygen carrier outlet, and the reducing oxygen carrier outlet of the fuel reactor 13 is connected to the reducing oxygen carrier inlet of the splitter 15 through a pipeline; the reducing oxygen carrier at the reducing oxygen carrier outlet of the fuel reactor 13 is divided into a first reducing oxygen carrier and a second reducing oxygen carrier in the splitter 15; The steam reactor 11 is provided with a reducing oxygen carrier inlet, a water vapor inlet, a partially oxidized reducing oxygen carrier outlet, and a hydrogen and water vapor outlet. The first reducing oxygen carrier of the diverter 15 is introduced into the steam reactor 11 through the reducing oxygen carrier inlet, and the water vapor at the water vapor outlet of the waste heat power generation unit 9 of the steam reactor is introduced into the steam reactor 11. The first reducing oxygen carrier and the water vapor undergo a partial oxidation reaction in the steam reactor 11 to generate hydrogen and water vapor as well as a partially oxidized reducing oxygen carrier. The air reactor 12 is provided with a partially oxidized reduced oxygen carrier inlet, a reduced oxygen carrier inlet, a hot air inlet, an oxygen carrier outlet and a nitrogen-rich gas outlet. The partially oxidized reduced oxygen carrier outlet of the steam reactor 11 is connected to the partially oxidized reduced oxygen carrier inlet of the air reactor 12 through a pipeline. The partially oxidized reduced oxygen carrier is introduced into the air reactor 12 through the partially oxidized reduced oxygen carrier inlet. The second reduced oxygen carrier at the reduced oxygen carrier outlet of the splitter 15 is introduced into the air reactor 12 through the reduced oxygen carrier inlet. The hot air at the hot air outlet of the air reactor waste heat power generation unit 8 is introduced into the air reactor 12 through the hot air inlet. The oxygen in the hot air oxidizes the second reduced oxygen carrier and the partially oxidized reduced oxygen carrier into oxygen carriers, and the oxygen carriers are transported to the fuel reactor 13 through a pipeline. The hot air consumes the oxygen to obtain nitrogen-rich gas, and the nitrogen-rich gas is input into the air reactor waste heat power generation unit 8 through the nitrogen-rich gas outlet.

[0024] The fuel reactor waste heat power generation unit 10 includes a first gas turbine 16, a second pump 17, a first heat exchanger 18, a first steam turbine unit 19, a first flash tank 20 and a first multi-stage compressor 21; The first gas turbine 16 is provided with a flue gas inlet and a flue gas outlet. The high-temperature flue gas from the flue gas outlet of the fuel reactor 13 is introduced into the gas turbine to generate electricity, and the remaining high-temperature flue gas is output from the flue gas outlet. The second pump 17 is provided with a water inlet and a water outlet. The second pump 17 pressurizes the water and delivers the pressurized water to the first heat exchanger 18. The first heat exchanger 18 is provided with a flue gas inlet, a water inlet, a flue gas outlet and a water vapor outlet. The water pressurized by the second pump 17 is passed into the first heat exchanger 18 through the water inlet. The high-temperature flue gas at the flue gas outlet of the first gas turbine 16 is passed into the first heat exchanger 18 through the flue gas inlet. In the first heat exchanger 18, the high-temperature flue gas exchanges heat with water to generate high-pressure steam. The first steam turbine unit 19 is provided with a high-pressure steam inlet. The high-pressure steam is passed into the first steam turbine unit 19 from the high-pressure steam inlet to perform work and generate electricity. The remaining flue gas in the first heat exchanger 18 is output from the flue gas outlet. The first flash tank 20 is provided with a flue gas inlet, a carbon dioxide gas outlet and a liquid mixture outlet. The remaining flue gas in the first heat exchanger 18 is input into the first flash tank 20 from the flue gas inlet. The flue gas is flashed through the first flash tank 20 to separate the gas and liquid to obtain CO and CO2. 2 mixture of gas and liquid phase; The first multi-stage compressor 21 is provided with a CO 2 Inlet and CO 2 outlet, CO2 gas outlet of the first flash tank 20 2 The gas is passed into the first multi-stage compressor 21 for pressurization.2 From CO 2 Export output.

[0025] The steam reactor waste heat power generation unit 9 includes a third pump 22, a second heat exchanger 23, a desulfurization device 24, a second steam turbine unit 25, a fourth pump 26, a third heat exchanger 27 and a second flash tank 28; The third pump 22 is provided with a water inlet and a water outlet. The third pump 22 pressurizes the water and delivers the pressurized water to the second heat exchanger 23. The second heat exchanger 23 is provided with a hydrogen and water vapor inlet, a water inlet, a hydrogen and water vapor outlet and a high-pressure steam outlet. The water of the third pump 22 is introduced into the second heat exchanger 23 through the water inlet. The hydrogen and water vapor outputted from the hydrogen and water vapor outlet of the steam reactor 11 are introduced into the second heat exchanger 23. The hydrogen and water vapor exchange heat with water in the second heat exchanger 23 to generate high-pressure steam and hydrogen and water vapor. The second steam turbine unit 25 is provided with a high-pressure steam inlet. The high-pressure steam is introduced into the second steam turbine unit 25 to generate electricity by performing work. The desulfurization device 24 is provided with a hydrogen and water vapor inlet and a hydrogen and water vapor outlet. The hydrogen and water vapor outlet of the second heat exchanger 23 is connected to the hydrogen and water vapor inlet of the desulfurization device 24 through a pipeline. The hydrogen and water vapor are introduced into the desulfurization device 24 containing the Fe2O3 and ZnO bed for desulfurization treatment. The fourth pump 26 is provided with a water inlet and a water outlet. The fourth pump 26 pressurizes the water and delivers the pressurized water to the third heat exchanger 27. The third heat exchanger 27 is provided with a hydrogen and water vapor inlet, a water inlet, a hydrogen and water vapor outlet, and a water vapor outlet. The hydrogen and water vapor outlet of the desulfurization device 24 is connected to the hydrogen and water vapor inlet of the third heat exchanger 27 through a pipeline. Hydrogen and water vapor exchange heat with water to generate water vapor and hydrogen and water vapor. The water vapor is introduced into the steam reactor 11 through the water vapor outlet. The second flash tank 28 is provided with a hydrogen and water vapor inlet, a hydrogen outlet and a water outlet. The hydrogen and water vapor outlet of the third heat exchanger 27 is connected to the hydrogen and water vapor inlet of the second flash tank 28 through a pipeline. The hydrogen and water vapor are separated by flash evaporation to obtain hydrogen and water.

[0026] The air reactor waste heat power generation unit 8 includes a second multi-stage compressor 29, a fourth heat exchanger 30, a fifth heat exchanger 31, a second gas turbine 32, a fifth pump 33 and a third steam turbine unit 34; The second gas turbine 32 is provided with a nitrogen-rich gas inlet and a nitrogen-rich gas outlet. The nitrogen-rich gas at the nitrogen-rich gas outlet of the air reactor 12 is introduced into the second gas turbine 32 to generate electricity, and the remaining nitrogen-rich gas is output from the nitrogen-rich gas outlet. The fifth pump 33 is provided with a water inlet and a water outlet. The fifth pump 33 pressurizes the water, and the pressurized water is input into the fourth heat exchanger 30. The fourth heat exchanger 30 is provided with a nitrogen-rich gas inlet, a water inlet, a nitrogen-rich gas outlet and a high-pressure steam outlet. The nitrogen-rich gas outlet of the second gas turbine 32 is connected to the nitrogen-rich gas inlet of the fourth heat exchanger 30 through a pipeline, and the nitrogen-rich gas exchanges heat with water to obtain high-pressure steam. The third steam turbine unit 34 is provided with a high-pressure steam inlet, and the high-pressure steam is introduced into the third steam turbine unit 34, and the high-pressure steam performs work in the third steam turbine unit 34 to generate electricity. The second multi-stage compressor 29 is provided with an air inlet and an air outlet, and the air is pressurized by the second multi-stage compressor 29 and output to the fifth heat exchanger 31; The fifth heat exchanger 31 is provided with an air inlet, a nitrogen-rich gas inlet, a hot air outlet and a nitrogen-rich gas outlet. The nitrogen-rich gas outlet of the fourth heat exchanger 30 is connected to the nitrogen-rich gas inlet of the fifth heat exchanger 31 through a pipeline. The air outlet of the second multi-stage compressor 29 is connected to the air inlet of the fifth heat exchanger 31 through a pipeline. The nitrogen-rich gas preheats the air in the fifth heat exchanger 31. The nitrogen-rich gas after heat exchange is output from the nitrogen-rich gas outlet, and the hot air is transported to the air reactor 12 through the hot air outlet.

[0027] like Figure 4 As shown, the synthetic ammonia unit 5 includes a third multi-stage compressor 35, a fourth multi-stage compressor 36, a first gas mixer 37, a deoxygenation reactor 38, a third flash tank 39, a first gas splitter 40, a second gas mixer 41, a sixth heat exchanger 42, a first synthetic ammonia reactor 43, a third gas mixer 44, a second synthetic ammonia reactor 45, a fourth gas mixer 46, a third synthetic ammonia reactor 47, a seventh heat exchanger 48, a second gas splitter 49, a compressor 50, an organic Rankine cycle device 51, a cooler 52, a fourth flash tank 53, and a fifth flash tank 54; The third multi-stage compressor 35 is provided with a hydrogen inlet and a hydrogen outlet. The hydrogen at the hydrogen outlet of the steam reactor waste heat power generation unit 9 is compressed in the first compressor, and the compressed hydrogen is output through the hydrogen outlet. The fourth multi-stage compressor 36 is provided with a nitrogen-rich gas inlet and a nitrogen-rich gas outlet. The nitrogen-rich gas outputted from the nitrogen-rich gas outlet of the fifth heat exchanger 31 is compressed in the fourth multi-stage compressor 36, and the compressed nitrogen-rich gas is outputted through the nitrogen-rich gas outlet. The first gas mixer 37 is provided with a nitrogen-rich gas inlet, a hydrogen inlet and a fresh synthesis gas outlet. The hydrogen at the hydrogen outlet of the third multi-stage compressor 35 and the nitrogen-rich gas at the nitrogen-rich outlet of the second compressor are respectively transported to the first gas mixer 37 through the hydrogen inlet and the nitrogen-rich gas inlet, mixed into fresh synthetic ammonia raw gas, and output from the fresh synthesis gas outlet. The deoxygenation reactor 38 is provided with a fresh synthetic ammonia raw gas inlet and a fresh synthetic ammonia raw gas outlet. The fresh synthetic ammonia raw gas at the fresh synthetic gas outlet of the first gas mixer 37 is input into the deoxygenation reactor 38 from the fresh synthetic ammonia raw gas inlet. After the fresh synthetic ammonia raw gas passes through the deoxygenation reactor 38 and is removed from oxygen, it is output from the fresh synthetic ammonia raw gas outlet into the third flash tank 39. The third flash tank 39 is provided with a fresh synthetic ammonia raw gas inlet, a fresh synthetic ammonia raw gas outlet and a water outlet. The fresh synthetic ammonia raw gas of the deoxygenation reactor 38 is introduced into the third flash tank 39 from the fresh synthetic ammonia raw gas inlet. The fresh synthetic ammonia raw gas is flashed to separate water and is output from the water outlet. The fresh synthetic ammonia raw gas after water separation is output through the fresh synthetic ammonia raw gas outlet. The second gas mixer 41 is provided with a fresh synthetic ammonia raw gas inlet, an unreacted gas inlet and a synthetic ammonia raw gas outlet. The fresh synthetic ammonia raw gas at the fresh synthetic ammonia raw gas outlet of the third flash tank 39 is input into the second gas mixer 41 through the fresh synthetic ammonia raw gas inlet, and the unreacted gas at the compressor outlet is introduced into the second gas mixer 41 through the unreacted gas inlet. The fresh synthetic ammonia raw gas and the unreacted gas are mixed into the synthetic ammonia raw gas and output through the synthetic ammonia raw gas outlet. The first gas splitter 40 is provided with a synthetic ammonia raw gas inlet, a first synthetic ammonia raw gas outlet, a second synthetic ammonia raw gas outlet and a third synthetic ammonia raw gas outlet. The synthetic ammonia raw gas at the synthetic ammonia raw gas outlet of the second gas mixer 41 is input into the first gas splitter 40 through the synthetic ammonia raw gas inlet. The synthetic ammonia raw gas is split into three synthetic ammonia raw gas streams in the first gas splitter 40, namely, the first synthetic ammonia raw gas, the second synthetic ammonia raw gas and the third synthetic ammonia raw gas. The sixth heat exchanger 42 is provided with a high-temperature mixed gas inlet, a first synthetic ammonia raw gas inlet, a high-temperature mixed gas outlet and a first synthetic ammonia raw gas outlet. The first synthetic ammonia raw gas of the first gas splitter 40 is introduced into the sixth heat exchanger 42 through the first synthetic ammonia raw gas inlet. The high-temperature mixed gas outputted from the third synthetic ammonia reactor 47 is introduced into the sixth heat exchanger 42 through the high-temperature mixed gas inlet of the sixth heat exchanger 42. In the sixth heat exchanger 42, the high-temperature mixed gas preheats the first synthetic ammonia raw gas. The first ammonia synthesis reactor 43 is provided with an ammonia synthesis raw gas inlet and a high-temperature mixed gas outlet. The first ammonia synthesis raw gas at the first ammonia synthesis raw gas outlet of the sixth heat exchanger 42 is introduced into the ammonia synthesis reactor through the ammonia synthesis raw gas inlet of the first ammonia synthesis reactor 43. The first ammonia synthesis raw gas generates a high-temperature mixed gas in the first ammonia synthesis reactor 43, and the high-temperature mixed gas is output from the high-temperature mixed gas outlet. The third gas mixer 44 is provided with a second synthetic ammonia raw gas inlet, a high-temperature mixed gas inlet and a synthetic ammonia mixed gas outlet. The high-temperature mixed gas output from the first synthetic ammonia reactor 43 is input into the third gas mixer 44 from the high-temperature mixed gas inlet. The second synthetic ammonia raw gas output from the first gas splitter 40 is transported into the third gas mixer 44 through the second synthetic ammonia raw gas inlet to be mixed into a synthetic ammonia mixed gas, which is then output from the synthetic ammonia mixed gas outlet. The second synthetic ammonia reactor 45 is provided with a synthetic ammonia mixed gas inlet and a high-temperature mixed gas outlet. The synthetic ammonia mixed gas at the synthetic ammonia mixed gas outlet of the third gas mixer 44 is input into the second synthetic ammonia reactor 45 through the synthetic ammonia mixed gas inlet. The synthetic ammonia mixed gas reacts in the second synthetic ammonia reactor 45 to generate a high-temperature mixed gas, which is output through the high-temperature mixed gas outlet. The fourth gas mixer 46 is provided with a third synthetic ammonia raw gas inlet, a high-temperature mixed gas inlet and a synthetic ammonia mixed gas outlet. The high-temperature mixed gas output from the second synthetic ammonia reactor 45 and the third synthetic ammonia raw gas output from the first gas splitter 40 are respectively introduced into the fourth gas mixer 46 through the high-temperature mixed gas inlet and the third synthetic ammonia raw gas inlet, and are mixed into a synthetic ammonia mixed gas and output through the synthetic ammonia mixed gas outlet. The third synthetic ammonia reactor 47 is provided with a synthetic ammonia mixed gas inlet and a high-temperature mixed gas outlet. The synthetic ammonia mixed gas outputted from the fourth gas mixer 46 is introduced into the third synthetic ammonia reactor 47. The synthetic ammonia mixed gas reacts in the third synthetic ammonia reactor 47 to generate a high-temperature mixed gas which is outputted through the high-temperature mixed gas outlet and introduced into the sixth heat exchanger 42 through the high-temperature mixed gas inlet of the sixth heat exchanger 42. The seventh heat exchanger 48 is provided with a high-temperature mixed gas inlet, an unreacted gas inlet, a high-temperature mixed gas outlet and an unreacted gas outlet. The high-temperature mixed gas outputted from the high-temperature mixer outlet of the sixth heat exchanger 42 is introduced into the seventh heat exchanger 48 through the high-temperature mixed gas inlet of the seventh heat exchanger 48. The unreacted gas outputted from the second flash tank 28 is introduced into the seventh heat exchanger 48 through the unreacted gas inlet. The high-temperature mixed gas and the unreacted gas exchange heat in the seventh heat exchanger 48. The high-temperature mixed gas preheats the unreacted gas. The high-temperature mixed gas and the unreacted gas outputted from the high-temperature mixed gas outlet and the unreacted gas outlet are introduced into the organic Rankine cycle device 51 and the second gas splitter 49 respectively. The second gas splitter 49 is provided with an unreacted gas inlet, a purge gas outlet and an unreacted gas outlet. The unreacted gas outputted from the seventh heat exchanger 48 is discharged from the second gas splitter 49 as purge gas and is outputted from the purge gas outlet. The remaining unreacted gas is outputted from the unreacted gas outlet and inputted into the compressor 50. The compressor 50 is provided with an unreacted gas inlet and an unreacted gas outlet. The unreacted gas outputted from the second gas splitter 49 is compressed by the compressor 50, and the pressurized unreacted gas is mixed with the fresh synthetic ammonia raw gas in the second gas mixer 41; The organic Rankine cycle device 51 includes a turbine 55, a condenser 56, a sixth pump 57 and an eighth heat exchanger 58. The sixth pump 57 is provided with a low-pressure refrigerant inlet and a high-pressure refrigerant outlet. The eighth heat exchanger 58 is provided with a high-temperature mixed gas inlet, a high-pressure refrigerant inlet, a mixed gas outlet and a high-pressure refrigerant outlet. The turbine 55 is provided with a high-pressure refrigerant inlet and a low-pressure refrigerant outlet. The condenser 56 is provided with a low-pressure refrigerant inlet and a low-pressure refrigerant outlet. The low-pressure refrigerant is introduced into the sixth pump 57, pressurized by the sixth pump 57 to obtain a high-pressure refrigerant, which is output through the high-pressure refrigerant outlet of the sixth pump 57, and introduced into the eighth heat exchanger 58 through the high-pressure refrigerant inlet of the eighth heat exchanger 58. The eighth heat exchanger The high-temperature mixed gas outputted from the heat exchanger 58 is introduced into the cooler 52 through the high-temperature mixed gas inlet of the eighth heat exchanger 58, and after heat exchange in the eighth heat exchanger 58, the mixed gas is outputted to the cooler 52 through the mixed gas outlet of the eighth heat exchanger 58, and the high-pressure refrigerant is outputted through the high-pressure refrigerant outlet of the eighth heat exchanger 58, and is inputted into the turbine 55 from the high-pressure refrigerant inlet of the turbine 55, and after power generation by the turbine 55, the low-pressure refrigerant is outputted through the low-pressure refrigerant outlet of the turbine 55, and the low-pressure refrigerant outputted from the low-pressure refrigerant outlet of the turbine 55 is introduced into the condenser 56 through the low-pressure refrigerant inlet of the condenser 56, and after being cooled by the condenser 56, the low-pressure refrigerant is outputted through the low-pressure refrigerant outlet of the condenser 56 and introduced into the sixth pump 57; The cooler 52 is provided with a mixed gas inlet and a mixed gas outlet. The mixed gas outputted from the mixed gas outlet of the eighth heat exchanger 58 of the organic Rankine cycle device 51 is passed into the cooler 52 from the mixed gas inlet. After the mixed gas is cooled, it is outputted through the mixed gas outlet. The fourth flash tank 53 is provided with a mixed gas inlet, an unreacted gas outlet and a crude ammonia product outlet. The mixed gas outputted from the mixed gas outlet of the cooler 52 is passed into the fourth flash tank 53 through the mixed gas inlet of the fourth flash tank 53. The mixed gas is separated into a crude ammonia product and unreacted gas by flash evaporation. The crude ammonia product and the unreacted gas are respectively outputted from the crude ammonia product outlet and the unreacted gas outlet. The unreacted gas is passed into the seventh heat exchanger 48 from the unreacted gas inlet of the seventh heat exchanger 48. The fifth flash tank 54 is provided with a crude ammonia product inlet, a liquid ammonia product outlet and a tail gas outlet. The crude ammonia product output from the crude ammonia product outlet of the fourth flash tank 53 is introduced into the crude ammonia product inlet of the fifth flash tank 54. The crude ammonia product is further flashed and separated in the fifth flash tank 54 to obtain a liquid ammonia product and part of the tail gas for discharge.

[0028] The mass ratio of the coal to high sulfur petroleum coke feed is 0.8 to 1.2.

[0029] The oxygen carrier material is Fe 2 O 3 With SiC, and Fe 2 O 3 Loaded on SiC at a mass ratio of 0.7 to 1.3.

[0030] In the chemical chain hydrogen production unit 7, the temperature of the fuel reactor 13 is 800 ~ 1000 ° C, and the pressure is 2 ~ 4 MPa, the temperature of the steam reactor 11 is 600 ~ 800 ° C, and the pressure is 2 ~ 4 MPa, and the temperature of the air fuel reactor 13 is 1200 ~ 1400 ° C, and the pressure is 2 ~ 4 MPa.

[0031] The hydrogen and rich nitrogen of the synthetic ammonia unit 5 are mixed at a molar ratio of 2.8 to 3.2 to form fresh synthetic ammonia raw gas; the feed temperature of the synthetic ammonia reactor is 300 to 500°C and the pressure is 18 to 22 MPa.

[0032] The liquid ammonia preparation system of the present invention comprises a chemical chain hydrogen production unit 7, an air reactor waste heat power generation unit 8, a steam reactor waste heat power generation unit 9, a fuel reactor waste heat power generation unit 10, and a synthetic ammonia unit 5. For specific connections and process flow charts, see Figure 2 .

[0033] The high sulfur petroleum coke and coal chemical chain ammonia production system of the present invention is Figure 1 The high sulfur petroleum coke and coal co-gasification ammonia production system shown is different in that: (1) The system of the present invention adopts chemical chain hydrogen production technology to avoid the high energy consumption of water gas conversion unit and acid gas removal unit in the high sulfur petroleum coke and coal co-gasification hydrogen production process, thereby improving the exergy efficiency of the high sulfur petroleum coke and coal chemical chain ammonia production system.

[0034] (2) The nitrogen of the synthetic ammonia unit 5 of the present invention is derived from the air reactor 12 of the air chemical chain hydrogen production unit 7, which is different from the nitrogen in the high-sulfur petroleum coke and coal co-gasification ammonia production process, which is derived from the air separation unit 6, thereby reducing the energy consumption of the system.

[0035] (3) The waste heat recovery method of the present invention adds a gas turbine and a steam turbine compared to the ORC device in the high-sulfur petroleum coke and coal co-gasification ammonia production process. Example

[0036] The specific implementation of the high sulfur petroleum coke and coal chemical chaining ammonia production process of this embodiment is as follows: The flow rate of the raw material high sulfur petroleum coke entering the process of the present invention is 25 t / h, the flow rate of the raw material coal is 25 t / h, and the feed mass ratio of high sulfur petroleum coke to coal is 1:1. The industrial analysis and elemental analysis of high sulfur petroleum coke and coal are shown in Table 1, and the general process flow diagram of high sulfur petroleum coke and coal chemical chain hydrogen production is shown in Figure 2 . Table 1 Industrial analysis and elemental analysis of high sulfur petroleum coke and coal

[0037] See the waste heat recovery process of high sulfur petroleum coke and coal hydrogen production unit and each reactor for details. Figure 3 , high-sulfur petroleum coke, water and oxygen carrier are transported to the fuel reactor 13 through a pipeline, the reaction temperature is 900 ℃, the pressure is 3 MPa, the reaction products are 900 ℃ flue gas mixture and 900 ℃ solid phase reduced oxygen carrier, the flue gas mixture enters the first gas turbine 16 to generate power, then enters the first heat exchanger 18 to exchange heat with water to generate steam, and enters the first steam turbine unit 19 to generate power. The flue gas mixture after heat exchange is flashed and separated from water in the first flash tank 20 to obtain pure carbon dioxide, and then CO 2 The compressed carbon dioxide is transported through a pipeline by the first multi-stage compressor 21 to 15 MPa. The reduced oxygen carrier is divided into two reduced oxygen carriers by a splitter. One part of the reduced oxygen carrier and water vapor enter the steam reactor 11. The reaction temperature is 750 ° C and the pressure is 3 MPa. The products are 750 ° C hydrogen and water vapor and 750 ° C The oxygen carrier is partially oxidized and reduced, and the hydrogen and water vapor are heat-exchanged with water in the second heat exchanger 23 to generate water vapor, which is then introduced into the second steam unit 25 to generate power. The hydrogen and water vapor at the outlet of the second heat exchanger 23 are then desulfurized by the desulfurization device 24 containing iron oxide and zinc oxide bed. The desulfurized hydrogen and water vapor are then heat-exchanged with water in the third heat exchanger 27 to generate water vapor, which is introduced into the steam reactor 11. The hydrogen and water vapor at the outlet of the third heat exchanger 27 are introduced into the second flash tank 28 to separate water. The hydrogen after flash dehydration is introduced into the next unit operation. Another part of the reduced oxygen carrier, part of the oxidized and reduced oxygen carrier and hot air are introduced into the air reactor 12. The reaction temperature is 1300°C and the pressure is 3 MPa. The product is 1300°C oxygen carrier and 1300 ℃, the nitrogen-rich gas is passed through the second gas turbine 32 to generate electricity, and the nitrogen-rich gas at its outlet is then heat exchanged with water in the fourth heat exchanger 30 to generate water vapor, which enters the third steam unit 34 to generate electricity, and the nitrogen-rich gas after heat exchange in the fourth heat exchanger 30 is then heat exchanged with the pressurized air in the fifth heat exchanger 31, and the air reactor 12 is self-heated by adjusting the air preheating temperature to 565 ℃.

[0038] Synthetic ammonia unit 5 process see Figure 4, hydrogen and nitrogen-rich gas are pressurized to 20.3 MPa by the third multi-stage compressor 35 and the fourth multi-stage compressor 36 respectively, and the pressurized hydrogen and nitrogen-rich gas are mixed in the first gas mixer 37 at a molar ratio of 3:1 to form fresh synthetic ammonia raw gas, the fresh synthetic ammonia raw gas is introduced into the deoxygenation reactor 38 to remove oxygen in the fresh synthetic ammonia raw gas, and then introduced into the third flash tank 39 to flash off a small amount of water in the fresh synthetic ammonia raw gas to obtain dry fresh synthetic ammonia raw gas, which is mixed with unreacted gas in the second gas mixer 41 to form synthetic ammonia raw gas, and is divided into three streams by the first splitter, namely the first synthetic ammonia raw gas, the second synthetic ammonia raw gas and the third synthetic ammonia raw gas, the first synthetic ammonia raw gas is preheated to 342°C in the sixth heat exchanger 42 by the high-temperature mixed gas at the outlet of the third synthetic ammonia reactor 47, and then introduced into the first synthetic ammonia reactor 43, the reaction temperature is 342°C, and the pressure is 20.3 MPa, the generated high-temperature mixed gas is mixed with the second synthetic ammonia raw gas in the third mixer 106 to form a synthetic ammonia mixed gas, and enters the second synthetic ammonia reactor 45, where the reaction temperature is 407°C and the pressure is 20.2 MPa. The generated gas phase high-temperature mixed gas is mixed with the third synthetic ammonia raw gas in the fourth gas mixer 46 to form a synthetic ammonia mixed gas, and enters the third synthetic ammonia reactor 47, where the reaction temperature is 400°C and the pressure is 20.1 MPa, and the reaction generates 400 ℃ high-temperature mixed gas, and preheat the first synthetic ammonia raw gas through the sixth heat exchanger 42, the high-temperature mixed gas after heat exchange and cooling is introduced into the seventh heat exchanger 48 to exchange heat with the unreacted gas at the outlet of the fourth flash tank 53, the unreacted gas heated in the seventh heat exchanger 48 is discharged in the second splitter as a purge gas, the remaining unreacted gas is pressurized by the compressor 50, the pressurized unreacted gas is introduced into the second mixer and mixed with the fresh synthetic ammonia raw gas to participate in the circulation reaction, the high-temperature mixed gas discharged from the seventh heat exchanger 48 is recovered through the organic Rankine device to recover heat and generate electricity, the mixed gas output from the mixed gas outlet of the eighth heat exchanger 58 of the organic Rankine device is cooled to -5 ℃ by the cooler 52, the mixed gas after cooling is separated from the unreacted gas and the crude ammonia product by the fourth flash tank 53, the crude ammonia product is then separated into the liquid ammonia product by flashing through the fifth flash tank 54, and part of the tail gas is discharged; The organic Rankine waste heat recovery device is the same as the prior art and can be implemented with reference to the description in the background technology.

[0039] Finally, compared with the high-sulfur petroleum coke and coal co-gasification ammonia production system, the exergy efficiency of the high-sulfur petroleum coke and coal chemical chaining system was increased from 47.72% to 51.05%, and the greenhouse gas emissions of the system were increased from 1368 kg CO 2 -eq / t NH 3 Reduced to 382 kg CO 2 -eq / t NH3 .

[0040] The above embodiments are preferred implementation modes of the present invention, but the implementation modes of the present invention are not limited to the above embodiments. Any other changes, modifications, substitutions, combinations, and simplifications that do not deviate from the spirit and principles of the present invention should be equivalent replacement methods and are included in the protection scope of the present invention.

Claims

1. A chemical chain ammonia production system using high-sulfur petroleum coke and coal as raw materials, Features: It includes a chemical chain hydrogen production unit, an air reactor waste heat power generation unit, a steam reactor waste heat power generation unit, a fuel reactor waste heat power generation unit and a synthetic ammonia unit; The chemical chaining hydrogen production unit is provided with a high-sulfur petroleum coke and coal inlet, a water vapor inlet, a water inlet, a hot air inlet, a flue gas outlet, a nitrogen-rich gas outlet, and a hydrogen and water vapor outlet. The high-sulfur petroleum coke and coal are introduced into the chemical chaining hydrogen production unit through the high-sulfur petroleum coke and coal inlets, the water vapor is introduced into the chemical chaining hydrogen production unit through the water vapor inlet, the water is introduced into the chemical chaining hydrogen production unit through the water inlet, and the hot air is introduced into the chemical chaining hydrogen production unit through the hot air inlet. The high-sulfur petroleum coke and coal, the water vapor, the water, and the hot air pass through the chemical chaining hydrogen production unit to obtain flue gas, nitrogen-rich gas, hydrogen, and water vapor. The air reactor waste heat power generation unit is provided with a nitrogen-rich gas inlet, a water inlet, an air inlet, an air outlet and a nitrogen-rich gas outlet. The nitrogen-rich gas outlet of the chemical chain hydrogen production unit is connected to the nitrogen-rich gas inlet of the air reactor waste heat power generation unit through a pipeline. The nitrogen-rich gas is introduced into the air reactor waste heat power generation unit through the nitrogen-rich gas inlet, the water is introduced into the air reactor waste heat power generation unit through the water inlet, and the air is introduced into the air reactor waste heat power generation unit through the air inlet. The nitrogen-rich gas is firstly generated by a gas turbine, and then heat-exchanged with water to obtain high-pressure steam. The high-pressure steam is generated by a steam turbine, and the nitrogen-rich gas after heat-exchange with water is preheated to the air. The air outlet of the air reactor waste heat power generation unit is connected to the air inlet of the chemical chain hydrogen production unit, and the preheated air is introduced into the chemical chain hydrogen production unit; the nitrogen-rich gas outlet of the air reactor waste heat power generation unit is connected to the nitrogen-rich gas inlet of the synthetic ammonia unit, and the nitrogen-rich gas is transported to the synthetic ammonia unit through a pipeline; The steam reactor waste heat power generation unit is provided with a water inlet, a hydrogen and water vapor inlet, a water vapor outlet and a hydrogen outlet. The hydrogen and water vapor outlet of the chemical chain hydrogen production unit is connected to the hydrogen and water vapor inlet of the steam reactor waste heat power generation unit through a pipeline. Water is introduced into the steam reactor waste heat power generation unit through the water inlet. Hydrogen and water vapor are introduced into the steam reactor waste heat power generation unit through the hydrogen and water vapor inlet. Hydrogen and water vapor are heat-exchanged with water to obtain high-pressure steam. The high-pressure steam is generated by a steam turbine. The cooled hydrogen and water vapor are heat-exchanged with water to obtain water vapor. The water vapor outlet of the steam reactor waste heat power generation unit is connected to the water vapor inlet of the chemical chain hydrogen production unit. The water vapor is introduced into the chemical chain hydrogen production unit through a pipeline. The hydrogen outlet of the steam reactor waste heat power generation unit is connected to the hydrogen inlet of the synthetic ammonia unit. The hydrogen is transported to the synthetic ammonia unit through a pipeline. The fuel reactor waste heat power generation unit is provided with a flue gas inlet, a water inlet and a CO 2 The flue gas outlet of the chemical chain hydrogen production unit is connected to the flue gas inlet of the fuel reactor waste heat power generation unit through a pipeline, the flue gas is introduced into the fuel reactor waste heat power generation unit through the flue gas inlet, and water is introduced into the fuel reactor waste heat power generation unit through the water inlet. The flue gas first passes through a gas turbine to generate electricity, and then exchanges heat with water to obtain high-pressure steam. The high-pressure steam generates electricity through a steam turbine, and the cooled flue gas is separated and dehydrated by flash evaporation to obtain high-purity CO 2 , and finally compressed to obtain high-pressure carbon dioxide, which is then passed through a pipeline from CO 2 Export output; The synthetic ammonia unit is provided with a nitrogen-rich gas inlet, a hydrogen inlet, a purge gas outlet and a liquid ammonia outlet. The hydrogen at the outlet of the steam reactor waste heat power generation unit and the nitrogen-rich gas in the air reactor waste heat power generation unit are respectively introduced into the synthetic ammonia unit through the hydrogen inlet and the nitrogen-rich gas inlet. The synthetic ammonia unit generates electricity and obtains purge gas and liquid ammonia, which are respectively output from the purge gas outlet and the liquid ammonia outlet.

2. A chemical chaining ammonia production system using high-sulfur petroleum coke and coal as raw materials according to claim 1, Features: The chemical chain hydrogen production unit comprises a steam reactor, an air reactor, a fuel reactor, a first pump and a flow divider; The first pump is provided with a water inlet and a water outlet, and the first pump pressurizes the water, and the pressurized water is delivered to the fuel reactor; The fuel reactor is provided with a high-sulfur petroleum coke and coal inlet, a water inlet, an oxygen carrier inlet, a flue gas outlet and a reduced oxygen carrier outlet. The water at the first water pump outlet is introduced into the fuel reactor through the water inlet, the oxygen carrier coming out of the air reactor is introduced into the fuel reactor through the oxygen carrier inlet, and the high-sulfur petroleum coke and coal are introduced into the fuel reactor through the high-sulfur petroleum coke and coal inlets. In the fuel reactor, the high-sulfur petroleum coke and coal, water and the oxygen carrier react to generate high-temperature flue gas and reduced oxygen carrier. The splitter is provided with a reducing oxygen carrier inlet and a reducing oxygen carrier outlet, and the reducing oxygen carrier outlet of the fuel reactor is connected to the reducing oxygen carrier inlet of the splitter through a pipeline; the reducing oxygen carrier at the reducing oxygen carrier outlet of the fuel reactor is divided into a first reducing oxygen carrier and a second reducing oxygen carrier in the splitter; The steam reactor is provided with a reducing oxygen carrier inlet, a water vapor inlet, a partially oxidized reducing oxygen carrier outlet and a hydrogen and water vapor outlet. The first reducing oxygen carrier of the diverter is introduced into the steam reactor through the reducing oxygen carrier inlet, and the water vapor at the water vapor outlet of the waste heat power generation unit of the steam reactor is introduced into the steam reactor. The first reducing oxygen carrier undergoes a partial oxidation reaction with the water vapor in the steam reactor to generate hydrogen and water vapor as well as the partially oxidized reducing oxygen carrier. The air reactor is provided with a partially oxidized reducing oxygen carrier inlet, a reducing oxygen carrier inlet, a hot air inlet, an oxygen carrier outlet and a nitrogen-rich gas outlet. The partially oxidized reducing oxygen carrier outlet of the steam reactor is connected to the partially oxidized reducing oxygen carrier inlet of the air reactor through a pipeline. The partially oxidized reducing oxygen carrier is introduced into the air reactor through the partially oxidized reducing oxygen carrier inlet. The second reducing oxygen carrier at the reducing oxygen carrier outlet of the splitter is introduced into the air reactor through the reducing oxygen carrier inlet. The hot air at the hot air outlet of the waste heat power generation unit of the air reactor is introduced into the air reactor through the hot air inlet. The oxygen in the hot air oxidizes the second reducing oxygen carrier and the partially oxidized reducing oxygen carrier into oxygen carriers, and the oxygen carrier is transported to the fuel reactor through a pipeline. The hot air consumes the oxygen to obtain nitrogen-rich gas, and the nitrogen-rich gas is input into the waste heat power generation unit of the air reactor through the nitrogen-rich gas outlet.

3. A chemical chaining ammonia production system using high-sulfur petroleum coke and coal as raw materials according to claim 2, Features: The fuel reactor waste heat power generation unit includes a first gas turbine, a second pump, a first heat exchanger, a first steam turbine unit, a first flash tank and a first multi-stage compressor; The first gas turbine is provided with a flue gas inlet and a flue gas outlet, the high-temperature flue gas at the flue gas outlet of the fuel reactor is introduced into the gas turbine to generate electricity, and the remaining high-temperature flue gas is output from the flue gas outlet; The second pump is provided with a water inlet and a water outlet, and the second pump pressurizes the water, and the pressurized water is transported to the first heat exchanger; The first heat exchanger is provided with a flue gas inlet, a water inlet, a flue gas outlet and a water vapor outlet. The water pressurized by the second pump is introduced into the first heat exchanger through the water inlet. The high-temperature flue gas at the flue gas outlet of the first gas turbine is introduced into the first heat exchanger through the flue gas inlet. In the first heat exchanger, the high-temperature flue gas exchanges heat with water to generate high-pressure steam. The first steam turbine unit is provided with a high-pressure steam inlet. The high-pressure steam is introduced into the first steam turbine unit from the high-pressure steam inlet to perform work and generate electricity. The remaining flue gas in the first heat exchanger is output from the flue gas outlet. The first flash tank is provided with a flue gas inlet, a CO 2 The remaining flue gas in the first heat exchanger is input into the first flash tank from the flue gas inlet. The flue gas is flashed through the first flash tank and the liquid is separated to obtain CO 2 mixture of gas and liquid phase; The first multi-stage compressor is provided with a CO 2 Inlet and CO 2 Export, first flash tank CO 2 CO at gas outlet 2 The gas is passed into the first multi-stage compressor for pressurization. 2 From CO 2 Export output.

4. A chemical chaining ammonia production system using high-sulfur petroleum coke and coal as raw materials according to claim 3, Features: The steam reactor waste heat power generation unit comprises a third pump, a second heat exchanger, a desulfurization device, a second steam turbine unit, a fourth pump, a third heat exchanger and a second flash tank; The third pump is provided with a water inlet and a water outlet, and the third pump pressurizes water, and the pressurized water is transported to the second heat exchanger; The second heat exchanger is provided with a hydrogen and water vapor inlet, a water inlet, a hydrogen and water vapor outlet and a high-pressure steam outlet. Water from the third pump is introduced into the second heat exchanger through the water inlet. The hydrogen and water vapor outputted from the hydrogen and water vapor outlet of the steam reactor are introduced into the second heat exchanger. The hydrogen and water vapor exchange heat with water in the second heat exchanger to generate high-pressure steam and hydrogen and water vapor. The second steam turbine unit is provided with a high-pressure steam inlet. The high-pressure steam is introduced into the second steam turbine unit to generate electricity by performing work. The desulfurization device is provided with a hydrogen and water vapor inlet and a hydrogen and water vapor outlet, the hydrogen and water vapor outlet of the second heat exchanger is connected to the hydrogen and water vapor inlet of the desulfurization device through a pipeline, and the hydrogen and water vapor are introduced into the desulfurization device for desulfurization treatment; The fourth pump is provided with a water inlet and a water outlet, and the fourth pump pressurizes the water, and the pressurized water is transported to the third heat exchanger; The third heat exchanger is provided with a hydrogen and water vapor inlet, a water inlet, a hydrogen and water vapor outlet, and a water vapor outlet. The hydrogen and water vapor outlet of the desulfurization device is connected to the hydrogen and water vapor inlet of the third heat exchanger through a pipeline. Hydrogen and water vapor exchange heat with water to generate water vapor and hydrogen and water vapor. The water vapor is introduced into the steam reactor through the water vapor outlet. The second flash tank is provided with a hydrogen and water vapor inlet, a hydrogen outlet and a water outlet. The hydrogen and water vapor outlet of the third heat exchanger is connected to the hydrogen and water vapor inlet of the second flash tank through a pipeline. The hydrogen and water vapor are separated by flash evaporation to obtain hydrogen and water.

5. A chemical chaining ammonia production system using high-sulfur petroleum coke and coal as raw materials according to claim 4, Features: The air reactor waste heat power generation unit comprises a second multi-stage compressor, a fourth heat exchanger, a fifth heat exchanger, a second gas turbine, a fifth pump and a third steam turbine unit; The second gas turbine is provided with a nitrogen-rich gas inlet and a nitrogen-rich gas outlet. The nitrogen-rich gas at the nitrogen-rich gas outlet of the air reactor is introduced into the second gas turbine to generate electricity, and the remaining nitrogen-rich gas is output from the nitrogen-rich gas outlet. The fifth pump is provided with a water inlet and a water outlet, and the fifth pump pressurizes the water, and the pressurized water is input into the fourth heat exchanger; The fourth heat exchanger is provided with a nitrogen-rich gas inlet, a water inlet, a nitrogen-rich gas outlet and a high-pressure steam outlet. The nitrogen-rich gas outlet of the second gas turbine is connected to the nitrogen-rich gas inlet of the fourth heat exchanger through a pipeline, and the nitrogen-rich gas exchanges heat with water to obtain high-pressure steam; the third steam turbine unit is provided with a high-pressure steam inlet, and the high-pressure steam is introduced into the third steam turbine unit, and the high-pressure steam performs work in the third steam turbine unit to generate electricity; The second multi-stage compressor is provided with an air inlet and an air outlet, and the air is pressurized by the second multi-stage compressor and output to the fifth heat exchanger; The fifth heat exchanger is provided with an air inlet, a nitrogen-rich gas inlet, a hot air outlet and a nitrogen-rich gas outlet. The nitrogen-rich gas outlet of the fourth heat exchanger is connected to the nitrogen-rich gas inlet of the fifth heat exchanger through a pipeline. The air outlet of the second multi-stage compressor is connected to the air inlet of the fifth heat exchanger through a pipeline. The nitrogen-rich gas preheats the air in the fifth heat exchanger, and the nitrogen-rich gas after heat exchange is output from the nitrogen-rich gas outlet. The hot air is transported to the air reactor through the hot air outlet.

6. A chemical chaining ammonia production system using high-sulfur petroleum coke and coal as raw materials according to claim 5, Features: The synthetic ammonia unit comprises a third multi-stage compressor, a fourth multi-stage compressor, a first gas mixer, a deoxygenation reactor, a third flash tank, a first gas splitter, a second gas mixer, a sixth heat exchanger, a first synthetic ammonia reactor, a third gas mixer, a second synthetic ammonia reactor, a fourth gas mixer, a third synthetic ammonia reactor, a seventh heat exchanger, a second gas splitter, a compressor, an organic Rankine cycle device, a cooler, a fourth flash tank, and a fifth flash tank; The third multi-stage compressor is provided with a hydrogen inlet and a hydrogen outlet, the hydrogen at the hydrogen outlet of the steam reactor waste heat power generation unit is compressed in the first compressor, and the compressed hydrogen is output through the hydrogen outlet; The fourth multi-stage compressor is provided with a nitrogen-rich gas inlet and a nitrogen-rich gas outlet, the nitrogen-rich gas outputted from the nitrogen-rich gas outlet of the fifth heat exchanger is compressed in the fourth multi-stage compressor, and the compressed nitrogen-rich gas is outputted through the nitrogen-rich gas outlet; The first gas mixer is provided with a nitrogen-rich gas inlet, a hydrogen inlet and a fresh synthesis gas outlet. The hydrogen at the hydrogen outlet of the third multi-stage compressor and the nitrogen-rich gas at the nitrogen-rich outlet of the second compressor are respectively transported to the first gas mixer through the hydrogen inlet and the nitrogen-rich inlet, mixed into fresh synthetic ammonia raw gas, and output from the fresh synthesis gas outlet. The deoxygenation reactor is provided with a fresh synthetic ammonia raw gas inlet and a fresh synthetic ammonia raw gas outlet. The fresh synthetic ammonia raw gas at the fresh synthetic gas outlet of the first gas mixer is input into the deoxygenation reactor from the fresh synthetic ammonia raw gas inlet. The fresh synthetic ammonia raw gas is deoxygenated in the deoxygenation reactor and then output into the third flash tank from the fresh synthetic ammonia raw gas outlet. The third flash tank is provided with a fresh synthetic ammonia raw gas inlet, a fresh synthetic ammonia raw gas outlet and a water outlet. The fresh synthetic ammonia raw gas of the deoxygenation reactor is introduced into the third flash tank from the fresh synthetic ammonia raw gas inlet. The fresh synthetic ammonia raw gas is flashed to separate water and output from the water outlet. The fresh synthetic ammonia raw gas after water separation is output through the fresh synthetic ammonia raw gas outlet. The second gas mixer is provided with a fresh synthetic ammonia raw gas inlet, an unreacted gas inlet and a synthetic ammonia raw gas outlet. The fresh synthetic ammonia raw gas at the fresh synthetic ammonia raw gas outlet of the third flash tank is input into the second gas mixer through the fresh synthetic ammonia raw gas inlet, and the unreacted gas at the compressor outlet is introduced into the second gas mixer through the unreacted gas inlet. The fresh synthetic ammonia raw gas and the unreacted gas are mixed into the synthetic ammonia raw gas and output through the synthetic ammonia raw gas outlet. The first gas splitter is provided with a synthetic ammonia raw gas inlet, a first synthetic ammonia raw gas outlet, a second synthetic ammonia raw gas outlet and a third synthetic ammonia raw gas outlet. The synthetic ammonia raw gas at the synthetic ammonia raw gas outlet of the second gas mixer is input into the first gas splitter through the synthetic ammonia raw gas inlet. In the first gas splitter, the synthetic ammonia raw gas is split into three synthetic ammonia raw gases, namely the first synthetic ammonia raw gas, the second synthetic ammonia raw gas and the third synthetic ammonia raw gas. The sixth heat exchanger is provided with a high-temperature mixed gas inlet, a first synthetic ammonia raw gas inlet, a high-temperature mixed gas outlet and a first synthetic ammonia raw gas outlet. The first synthetic ammonia raw gas of the first gas splitter is introduced into the sixth heat exchanger through the first synthetic ammonia raw gas inlet. The high-temperature mixed gas outputted from the third synthetic ammonia reactor is introduced into the sixth heat exchanger through the high-temperature mixed gas inlet of the sixth heat exchanger. In the sixth heat exchanger, the high-temperature mixed gas preheats the first synthetic ammonia raw gas. The first ammonia synthesis reactor is provided with an ammonia synthesis raw gas inlet and a high-temperature mixed gas outlet. The first ammonia synthesis raw gas at the first ammonia synthesis raw gas outlet of the sixth heat exchanger is introduced into the ammonia synthesis reactor through the ammonia synthesis raw gas inlet of the first ammonia synthesis reactor. The first ammonia synthesis raw gas generates a high-temperature mixed gas in the first ammonia synthesis reactor, and the high-temperature mixed gas is output from the high-temperature mixed gas outlet. The third gas mixer is provided with a second synthetic ammonia raw gas inlet, a high-temperature mixed gas inlet and a synthetic ammonia mixed gas outlet. The high-temperature mixed gas output from the first synthetic ammonia reactor is input into the third gas mixer from the high-temperature mixed gas inlet. The second synthetic ammonia raw gas output from the first gas splitter is transported into the third gas mixer through the second synthetic ammonia raw gas inlet to be mixed into a synthetic ammonia mixed gas. The synthetic ammonia mixed gas is output from the synthetic ammonia mixed gas outlet. The second ammonia synthesis reactor is provided with an ammonia mixture inlet and a high-temperature mixed gas outlet. The ammonia mixture at the ammonia mixture outlet of the third gas mixer is input into the second ammonia synthesis reactor through the ammonia mixture inlet. The ammonia mixture reacts in the second ammonia synthesis reactor to generate a high-temperature mixed gas, and the high-temperature mixed gas is output through the high-temperature mixed gas outlet. The fourth gas mixer is provided with a third synthetic ammonia raw gas inlet, a high-temperature mixed gas inlet and a synthetic ammonia mixed gas outlet. The high-temperature mixed gas output from the second synthetic ammonia reactor and the third synthetic ammonia raw gas output from the first gas splitter are respectively introduced into the fourth gas mixer through the high-temperature mixed gas inlet and the third synthetic ammonia raw gas inlet, and are mixed into a synthetic ammonia mixed gas and output through the synthetic ammonia mixed gas outlet. The third synthetic ammonia reactor is provided with a synthetic ammonia mixed gas inlet and a high-temperature mixed gas outlet. The synthetic ammonia mixed gas outputted from the fourth gas mixer is introduced into the third synthetic ammonia reactor. In the third synthetic ammonia reactor, the synthetic ammonia mixed gas reacts to generate a high-temperature mixed gas which is outputted through the high-temperature mixed gas outlet and introduced into the sixth heat exchanger through the high-temperature mixed gas inlet of the sixth heat exchanger. The seventh heat exchanger is provided with a high-temperature mixed gas inlet, an unreacted gas inlet, a high-temperature mixed gas outlet and an unreacted gas outlet. The high-temperature mixed gas outputted from the high-temperature mixer outlet of the sixth heat exchanger is introduced into the seventh heat exchanger through the high-temperature mixed gas inlet of the seventh heat exchanger. The unreacted gas outputted from the second flash tank is introduced into the seventh heat exchanger through the unreacted gas inlet. The high-temperature mixed gas and the unreacted gas exchange heat in the seventh heat exchanger. The high-temperature mixed gas preheats the unreacted gas. The high-temperature mixed gas and the unreacted gas outputted from the high-temperature mixed gas outlet and the unreacted gas outlet are introduced into the organic Rankine cycle device and the second gas splitter respectively. The second gas splitter is provided with an unreacted gas inlet, a purge gas outlet and an unreacted gas outlet, the unreacted gas outputted by the seventh heat exchanger is outputted from the purge gas outlet as purge gas at the discharge portion of the second gas splitter, and the remaining unreacted gas is outputted from the unreacted gas outlet and inputted into the compressor; The compressor is provided with an unreacted gas inlet and an unreacted gas outlet, the unreacted gas outputted by the second gas splitter is compressed by the compressor, and the pressurized unreacted gas is mixed with the fresh synthetic ammonia raw gas in the second gas mixer; The organic Rankine cycle device includes a turbine, a condenser, a sixth pump and an eighth heat exchanger. The sixth pump is provided with a low-pressure refrigerant inlet and a high-pressure refrigerant outlet. The eighth heat exchanger is provided with a high-temperature mixed gas inlet, a high-pressure refrigerant inlet, a mixed gas outlet and a high-pressure refrigerant outlet. The turbine is provided with a high-pressure refrigerant inlet and a low-pressure refrigerant outlet. The condenser is provided with a low-pressure refrigerant inlet and a low-pressure refrigerant outlet. The low-pressure refrigerant is introduced into the sixth pump, pressurized by the sixth pump to obtain a high-pressure refrigerant, which is output through the high-pressure refrigerant outlet of the sixth pump, and introduced into the eighth heat exchanger through the high-pressure refrigerant inlet of the eighth heat exchanger. The high-temperature mixed gas outputted from the eight heat exchangers is introduced through the high-temperature mixed gas inlet of the eighth heat exchanger, and after heat exchanged by the eighth heat exchanger, the mixed gas is outputted to the cooler through the mixed gas outlet of the eighth heat exchanger, and the high-pressure refrigerant is outputted through the high-pressure refrigerant outlet of the eighth heat exchanger, and is inputted into the turbine from the high-pressure refrigerant inlet of the turbine, and after power generation by the turbine, the low-pressure refrigerant is outputted through the low-pressure refrigerant outlet of the turbine, and the low-pressure refrigerant outputted from the low-pressure refrigerant outlet of the turbine is introduced into the condenser through the low-pressure refrigerant inlet of the condenser, and after being cooled by the condenser, the low-pressure refrigerant is outputted through the low-pressure refrigerant outlet of the condenser and introduced into the sixth pump; The cooler is provided with a mixed gas inlet and a mixed gas outlet. The mixed gas outputted from the mixed gas outlet of the eighth heat exchanger of the organic Rankine cycle device is passed into the cooler from the mixed gas inlet of the cooler. After the mixed gas is cooled, it is outputted through the mixed gas outlet. The fourth flash tank is provided with a mixed gas inlet, an unreacted gas outlet and a crude ammonia product outlet. The mixed gas outputted from the mixed gas outlet of the cooler is introduced into the fourth flash tank through the mixed gas inlet of the fourth flash tank. The mixed gas is separated into a crude ammonia product and unreacted gas by flash evaporation. The crude ammonia product and the unreacted gas are respectively outputted from the crude ammonia product outlet and the unreacted gas outlet. The unreacted gas is introduced into the seventh heat exchanger from the unreacted gas inlet of the seventh heat exchanger. The fifth flash tank is provided with a crude ammonia product inlet, a liquid ammonia product outlet and a tail gas outlet. The crude ammonia product output from the crude ammonia product outlet of the fourth flash tank is introduced into the crude ammonia product inlet of the fifth flash tank. The crude ammonia product is further flashed and separated in the fifth flash tank to obtain a liquid ammonia product and part of the tail gas for discharge.

7. A chemical chaining ammonia production system using high-sulfur petroleum coke and coal as raw materials according to claim 1, Features: The mass ratio of the coal to high sulfur petroleum coke feed is 0.8 to 1.

2.

8. A chemical chaining ammonia production system using high-sulfur petroleum coke and coal as raw materials according to claim 2, Features: The oxygen carrier material is Fe 2 O 3 With SiC, and Fe 2 O 3 Loaded on SiC at a mass ratio of 0.7 to 1.

3.

9. A chemical chaining ammonia production system using high-sulfur petroleum coke and coal as raw materials according to claim 2, Features: The temperature of the fuel reactor in the chemical chain hydrogen production unit is 800 ~ 1000 ° C, the pressure is 2 ~ 4 MPa, the temperature of the steam reactor is 600 ~ 800 ° C, the pressure is 2 ~ 4 MPa, and the temperature of the air fuel reactor is 1200 ~ 1400 ° C, the pressure is 2 ~ 4 MPa.

10. A chemical chaining ammonia production system using high-sulfur petroleum coke and coal as raw materials according to claim 6, Features: The hydrogen and rich nitrogen of the synthetic ammonia unit are mixed at a molar ratio of 2.8 to 3.2 to form fresh synthetic ammonia raw gas; the feed temperature of the synthetic ammonia reactor is 300 to 500°C and the pressure is 18 to 22 MPa.

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