A system for producing green hydrogen from phenol tar

Abstract

This invention discloses a system for producing green hydrogen from phenol tar. A feed oil buffer tank is connected to pipelines 19 and 18 via phenol-acetone tar feed pumps. The feed oil buffer tank also has pipelines 1 and 2. A feed oil circulation pump and a feed oil pump are sequentially connected to the bottom of the feed oil buffer tank. After passing through the feed oil pump, the feed oil enters the top of the gasifier. The quench chamber inside the gasifier is connected to the top of a carbon black quench tube. The bottom of the carbon black quench tube is connected to a carbon black separator. The top of the carbon black separator is connected to the lower part of a washing tower, and the bottom of the carbon black separator is connected to the gasifier. Pipeline 12 is connected to the upper part of the carbon black quench tube. A quench water pump is connected to the bottom of the washing tower and is connected to pipeline 12. A cold water pump and pipeline 12 converge and connect to the washing tower. The washing water pump is connected to the gasifier, and the top of the washing tower is connected to a methanol washing tower. This system can recycle waste materials, reduce water and energy consumption, increase product gas, and has broad market application prospects.

Description

Technical Field

[0001] This invention relates to a system, and more specifically, to a system for producing green hydrogen from phenol tar, belonging to the field of petrochemicals. Background Technology

[0002] Phenol tar is a byproduct of the co-production of phenol and acetone using the cumene process. Approximately 0.11 tons of phenol tar are produced for every ton of phenol produced. Phenol tar has a complex composition, mainly containing phenol, acetophenone, 4-cumylphenol, 2,4-diphenyl-4-methyl-1-pentene, 2,4-dicumylphenol, UIRES, m-cresol, p-cresol, 2-phenylpropanal, and dimethylbenzyl alcohol. Phenol tar contains approximately 35% light components, with the remainder being heavy components. It is classified as HW11 hazardous waste in the hazardous waste catalog. Separation and recovery are energy-intensive. Traditionally, its use as fuel not only wastes energy but also results in low combustion temperatures, incomplete decomposition, and environmental pollution.

[0003] Practical experience has shown that blending phenol tar into EST residue and vacuum residue, and controlling the appropriate proportions, temperature, pressure, and pure oxygen in a Shell heavy oil gasifier for a partial oxidation reaction, produces syngas primarily composed of carbon monoxide and hydrogen. After washing, cooling, shift conversion, and purification, pure hydrogen is obtained, with a carbon conversion rate exceeding 98%. All production wastewater meets environmental protection standards. This method can harmlessly treat phenol tar and yield pure hydrogen. Phenol tar has a low initial boiling point, low viscosity, and low ash content, reducing system steam consumption and water circulation compared to the original feedstock, thus achieving energy saving and consumption reduction. Summary of the Invention

[0004] To address the aforementioned problems, the present invention provides a system capable of producing green hydrogen from phenol tar.

[0005] To achieve the above objectives, the present invention is implemented through the following technical solution:

[0006] This invention discloses a system for producing green hydrogen from phenol tar, comprising a feed oil buffer tank V-01 and a phenol-acetone tar buffer tank V-04. The feed oil buffer tank V-04 is connected to pipelines No. 19 and No. 18 via a phenol-acetone tar feed pump P-07. Pipelines No. 1 and No. 2 are located on the side of the feed oil buffer tank V-01, and pipelines No. 19 and No. 18 are connected to pipelines No. 1 and No. 2, respectively. The bottom of the feed oil buffer tank V-01 is connected to pipeline No. 23. There is a feed oil circulation pump P-01, and the feed oil circulation pump P-01 is connected to a feed oil pump P-02 via pipeline No. 23. After being pressurized by the feed oil pump P-02, it is connected to the process burner at the top of the gasifier R-01 via pipeline No. 4. The quench chamber inside the gasifier R-01 is connected to the top of the carbon black quench tube V-02 via pipeline No. 5. The bottom of the carbon black quench tube V-02 is connected to the carbon black separator V-03 via pipeline No. 6. The top of the carbon black separator V-03 is connected to... At the bottom of the scrubbing tower C-01, the bottom of the carbon black separator V-03 is connected to the gasifier R-01 via pipeline No. 17, which includes a black water pump P-04. The upper part of the carbon black quench pipe V-02 is connected to pipeline No. 12, which includes a quench water flow regulating valve FV-12. The bottom of the scrubbing tower C-01 is connected to a quench water pump P-06, which is connected to pipeline No. 12. The cold water pump P-06 and pipeline No. 12 converge and are then connected to the upper part of C-01 via pipeline No. 11 for spraying. It also includes a washing water pump P-05, which is connected to the gasifier R-01 via pipeline No. 14 and to the upper part of the washing tower C-01 via pipeline No. 15. The top of the washing tower C-01 is connected to the methanol washing tower C-02 via pipeline No. 8. Pipeline No. 8 controls the pressure of the gasification system and sends the syngas to the shift reactor R-02 to convert CO in the syngas into H2. Then, the hydrogen is sent to the methanol washing tower C-02 for desulfurization and decarbonization. After the syngas is converted and purified, pure hydrogen is obtained.

[0007] Preferably, the top burner of the gasifier R-01 is also connected to a third pipeline equipped with an oxygen flow regulating valve FV-03. The oxygen enters the gasifier R-01 through the process burner for reaction. The ratio of oxygen from the third and fourth pipelines is controlled to enter the process burner of the gasifier R-01 for reaction. The oxygen flow regulating valve FV-03 regulates the oxygen flow into the gasifier, and the flow rate of the fourth pipeline is regulated by the feed oil pump P-02 via frequency conversion. The oxygen flow and feed oil flow are strictly controlled proportionally, with the methane composition in the synthesis gas serving as the control target, forming an automatic control loop.

[0008] Preferably, the carbon black quench pipe V-02 is connected to a spray water pump P-03 via a No. 9 pipeline equipped with a spray water flow regulating valve FV-09; and a regulating valve FV-24 is connected between the No. 23 pipeline and the feed oil buffer tank V-01.

[0009] Preferably, the No. 1, No. 23, and No. 4 pipelines are equipped with patch heat tracing, and the patch heat tracing temperature is not lower than 220°C, so as to ensure the fluidity of the raw materials and ensure that the medium temperature does not drop for two hours after the heat tracing steam stops.

[0010] Preferably, the flow rate ratio of the fourth pipeline to the third pipeline is controlled, and the mass ratio is controlled between 0.9 and 1.3.

[0011] Preferably, the No. 1 pipeline is equipped with a slurry valve to ensure that the valve has no dead zone and that high-viscosity oil does not clog; the No. 1 pipeline and the No. 2 pipeline are respectively connected to an EST oil residue regulating valve FV-01 and a pressure reducing residue oil flow regulating valve FV-02.

[0012] Preferably, both pipelines 19 and 18 are connected to pipeline 20, which is equipped with a phenol-acetone pressure regulating valve PV-20. Pipeline 20 is a return line, which is connected to the phenol-acetone tar buffer tank V-04 to regulate the phenol tar supply pressure and ensure that the phenol tar is smoothly incorporated into the EST oil residue.

[0013] Preferably, the No. 2 pipeline transports depressurized residue oil, the No. 18 pipeline is adjusted and connected to the No. 2 pipeline through the shut-off valve 1, the No. 19 pipeline is connected to the No. 1 pipeline through the shut-off valve 2 in proportion, and the connection pressure is adjusted through the No. 20 pipeline.

[0014] Preferably, the feed oil buffer tank V-01 is connected to pipeline No. 21 and pipeline No. 22. Pipeline No. 21 is connected to the feed oil buffer tank pressurization valve PV-21 to pressurize with medium-pressure nitrogen, and pipeline No. 22 is connected to the feed oil buffer tank pressure relief valve PV-22 to relieve pressure. The pressure of the feed oil buffer tank V-01 is controlled at 0.7MPa to ensure the inlet flow rate of the feed oil circulation pump P-01 and avoid pipeline blockage.

[0015] Preferably, the syngas in the gasifier combustion chamber is introduced into the quench chamber water bath through a downcomer. A quench ring is provided at the top of the downcomer, and quench water is sprayed at an angle. Pipeline No. 14 is connected to the quench ring, and an ascender is provided outside the quench ring to ensure full contact between the syngas and the quench chamber water bath and reduce water carryover in the syngas. The syngas in the quench chamber is sent to the top of the quench chamber through the ascender. Spray water is provided at the syngas outlet, and a spray water distribution device is provided. After being wetted by the spray water, the syngas is sent out of the gasifier through pipeline No. 5.

[0016] Pipelines No. 3 and No. 4 enter the gasifier, where an incomplete oxidation reaction occurs. Approximately 92% effective gas, CO + H2, is produced in gasifier R-01.

[0017]

[0018]

[0019] A cold water supply line is connected to the bottom of the gasifier R-01. Pipelines No. 14 and No. 17 enter the bottom of the gasifier to cool and wash the syngas. Pipelines No. 12 and No. 9 are connected to the carbon black quench pipe V-02 for further washing of the syngas. Pipeline No. 6 is connected to the carbon black separator V-03. After separation, the gas phase pipeline No. 7 enters the bottom of the scrubbing tower C-01. After separation, the liquid phase pipeline No. 16 is connected to the gasifier R-01. Pipeline No. 15 is connected to the upper part of the scrubbing tower C-01 to wash the syngas and form saturated water gas.

[0020] Beneficial effects: It enables the recycling of waste materials, reduces water and energy consumption, increases product gas production, and has broad market application prospects. The unit's product scale is 140,000 Nm³ of effective gas (H2) produced from oil residue gasification. 3 / h, with a final hydrogen-rich product capacity of 141,000 Nm³. 3 / h. Firing 3.5 tons of phenol-acetone tar per hour can increase production by approximately 9245 Nm³. 3 / h hydrogen. Attached Figure Description

[0021] Figure 1 This is a schematic diagram of the structure of the present invention.

[0022] In the diagram: R-01: Gasifier, R-02: Shift converter, V-01: Feed oil buffer tank, V-02: Carbon black quench tube, V-03: Carbon black separator, V-04: Phenol-acetone tar buffer tank, C-01: Scrubber, C-02: Methanol scrubber, P-01: Feed oil circulation pump, P-02: Feed oil pump, P-03: Spray water pump, P-04: Black water pump, P-05: Scrub water pump, P-06: Quenching water pump, P-07: Phenol-acetone tar feed pump, FV-01: EST residue regulating valve, FV-02: Pressure reducing residue oil flow regulating valve, FV- 03: Oxygen flow regulating valve; FV-09: Spray water flow regulating valve; FV-12: Quenching water flow regulating valve; FV-11: Quenching water circulation regulating valve; FV-14: Gasifier washing water flow regulating valve; FV-15: Scrubber washing water flow regulating valve; FV-17: Black water flow regulating valve; PV-20: Phenol and acetone pressure regulating valve; PV-21: Feed oil buffer tank pressurization valve; PV-22: Feed oil buffer tank pressure relief valve; Hand valve 1, shut-off valve 1: Phenol, acetone, tar and EST slag oil hand valve; Hand valve 2, shut-off valve 2: Phenol, acetone, tar and EST slag reduction hand valve. Detailed Implementation

[0023] The present invention will be further described below with reference to the accompanying drawings, but the present invention is not limited to the following embodiments.

[0024] like Figure 1The diagram illustrates a specific example of a system for producing green hydrogen from phenol tar. In this system, the upper part of the feed oil buffer tank V-01 is connected to pipelines No. 1 and No. 2, whose flow rates are regulated by FV-01 and FV-02 respectively, leading to the feed oil entering the feed oil buffer tank V-01. Pipeline No. 23 is connected to the bottom of the feed oil buffer tank V-01, where it is pressurized by the feed oil circulation pump P-01. Pipeline No. 23 is connected to the feed oil pump P-02, and the feed oil flows through the feed oil circulation pump P-02... After being pressurized by the oil pump P-02, the return flow rate is regulated by FV-24. Pipeline 4 is connected to the top burner of gasifier R-01. Pipeline 3 is connected to the top process burner of gasifier R-01. The flow rate is regulated by FV-03 and enters the gasifier R-01 for reaction. Pipeline 5 is connected to the lower part of gasifier R-01 and to the top of carbon black quench tube V-02. Pipeline 6 is connected to the bottom of carbon black separator V-03 and is also connected to carbon black separator V-03. Pipeline 7... The pipeline is connected to the bottom of the carbon black washing tower. Pipeline 14, after its flow rate is adjusted by flow regulating valve FV-14, is connected to the quench ring of the quench chamber in gasifier R-01. Pipeline 17 is connected to the bottom of gasifier R-01. Pipeline 12, after adjustment by FV-12, is connected to the upper part of carbon black quench pipe V-02. Pipeline 9, after adjustment by FV-09, is connected to the middle of carbon black quench pipe V-02. Pipeline 11, through FV-11, regulates the quench water pump return flow. Pipeline 15... Connected to the upper part of the scrubbing tower C-01, the scrubbing water is sent to the upper part of the scrubbing tower C-01 by adjusting FV-15. The nineteenth pipeline is connected to the first pipeline through the shut-off valve 2 in proportion. The eighteenth pipeline is connected to the second pipeline through the shut-off valve 2 in proportion. The third and fourth pipelines are controlled to enter the gasifier burner in proportion and react in the gasifier. The eighth pipeline controls the pressure of the gasification system and sends the syngas to the conversion. After conversion and purification, the syngas is purified to obtain pure hydrogen.

[0025] Specific implementation methods:

[0026] 1. Feeding process

[0027] EST oil residue enters feed oil buffer tank V-01 after flow adjustment via FV-01, and vacuum residue enters feed oil buffer tank V-01 after flow adjustment via FV-02. The ratio of EST oil residue to vacuum residue is controlled according to calculated data, enabling feeding based on the ratio and adjustment as needed. Phenol-acetone tar is pressurized from phenol-acetone tar buffer tank V-04 via phenol-acetone tar feed pump P-07 and controlled by pressure regulating valve PV-20. The pressure is adjusted, and the phenol-acetone tar is divided into two streams. One stream is mixed with the pressure-reducing residue oil through shut-off valve 1, and the other stream is mixed with the EST oil residue through shut-off valve 2. The mixing ratio is adjusted and the mixture enters the feed oil buffer tank. The mixed raw materials in the feed oil buffer tank are pressurized by the feed oil circulation pump P-01 and boosted by the feed oil pump P-02 before being sent to the gasifier. The phenol-acetone tar has good fluidity, and the system feed temperature is controlled at a low level, which reduces the amount of steam used. The phenol-acetone tar has low viscosity, and the flow rate can be controlled at a low level, which can reduce the operating pressure.

[0028] 2. Reaction control process

[0029] The mixed feedstock oil is pressurized by P-02, which is also a variable frequency pump. The flow rate is adjusted by frequency conversion. The oxygen flow rate is adjusted by FV-03. The oxygen-oil ratio is controlled precisely. Precise oxygen-oil ratio control is the key to the safe operation of the gasifier and an important means to control the gasification reaction efficiency.

[0030] The high-temperature syngas from the gasifier undergoes preliminary washing and cooling via water from black water pump P-04 and washing water pump P-05. After exiting the gasifier, the syngas enters the carbon black quench tube, where it is further washed and cooled by water supplied by quench water pump P-06 and spray water pump P-03. The cooled syngas then enters the carbon black separator V-03, which separates the free water from the syngas. The gas phase enters the bottom of the washing tower C-01, while the liquid phase circulates back to the gasifier. In the washing tower C-01, the syngas is thoroughly washed from bottom to top by the washing water supplied by the washing water pump. The outlet pressure of the washing tower is controlled by PV-01, which controls the pressure of the gasification system, thereby controlling the reaction residence time in the gasifier and ensuring gasification efficiency. The phenol, acetone, and tar have low ash content, resulting in low washing water consumption and saving on electricity and water treatment costs.

[0031] Syngas is washed and then sent to shift converter R-02 and methanol washing tower C-02 for conversion, purification and upgrading to produce pure hydrogen.

[0032] In a preferred embodiment, the top burner of the gasifier R-01 is also connected to a third pipeline equipped with an oxygen flow regulating valve FV-03. The oxygen enters the gasifier R-01 through the process burner for reaction. The ratio of oxygen from the third and fourth pipelines to the process burners in the gasifier R-01 is controlled, and the reaction occurs within the gasifier R-01. The oxygen flow regulating valve FV-03 regulates the oxygen flow into the gasifier, and the flow rate of the fourth pipeline is regulated by a frequency converter via the feed oil pump P-02. The oxygen flow and feed oil flow are strictly controlled proportionally, with the methane composition in the syngas serving as the control target, forming an automatic control loop.

[0033] In a preferred embodiment, the carbon black quench pipe V-02 is connected to a spray water pump P-03 via a No. 9 pipeline equipped with a spray water flow regulating valve FV-09; and a regulating valve FV-24 is connected between the No. 23 pipeline and the feed oil buffer tank V-01.

[0034] In a preferred embodiment, the No. 1, No. 23, and No. 4 pipelines are equipped with patch heat tracing, and the patch heat tracing temperature is not lower than 220°C, so as to ensure the fluidity of the raw materials and ensure that the medium temperature does not drop for two hours after the heat tracing steam stops.

[0035] In a preferred embodiment, the flow rate ratio between pipeline No. 4 and pipeline No. 3 is controlled, with the mass ratio controlled between 0.9 and 1.3, preferably between 1.1.

[0036] In a preferred embodiment, the first pipeline 1 is equipped with a slurry valve to ensure that the valve has no dead zone and that high-viscosity oil does not clog; the first pipeline and the second pipeline are respectively connected to an EST oil residue regulating valve FV-01 and a pressure reducing residue oil flow regulating valve FV-02.

[0037] In a preferred embodiment, both pipelines 19 and 18 are connected to pipeline 20, which is equipped with a phenol-acetone pressure regulating valve PV-20. Pipeline 20 is a return line and is connected to the phenol-acetone tar buffer tank V-04 to regulate the phenol tar supply pressure and ensure that the phenol tar is smoothly incorporated into the EST sludge.

[0038] In a preferred embodiment, pipeline number two transports depressurized residue oil, pipeline number eighteen is connected to pipeline number two via shut-off valve 1, and pipeline number nineteen is connected to pipeline number one via shut-off valve 2 in proportion, and the connection pressure is adjusted via pipeline number twenty.

[0039] In a preferred embodiment, the feed oil buffer tank V-01 is connected to pipeline No. 21 and pipeline No. 22. Pipeline No. 21 is connected to the feed oil buffer tank pressurization valve PV-21 to pressurize with medium-pressure nitrogen, and pipeline No. 22 is connected to the feed oil buffer tank pressure relief valve PV-22 to relieve pressure. The pressure of the feed oil buffer tank V-01 is controlled at 0.7MPa to ensure the inlet flow rate of the feed oil circulation pump P-01 and avoid pipeline blockage.

[0040] In a preferred embodiment, the syngas in the gasifier combustion chamber is introduced into the quench chamber water bath through a downcomer. A quench ring is provided at the top of the downcomer, and quench water is sprayed at an angle. Pipeline No. 14 is connected to the quench ring, and an ascender is provided outside the quench ring to ensure full contact between the syngas and the quench chamber water bath, reducing water carryover in the syngas. The syngas in the quench chamber is sent to the top of the quench chamber through the ascender, and spray water is provided at the syngas outlet. A spray water distribution device is provided, and after being wetted by the spray water, the syngas is sent out of the gasifier through pipeline No. 5.

[0041]

[0042]

[0043] Pipelines No. 3 and No. 4 enter the gasifier, where an incomplete oxidation reaction occurs, with I2 being the main reaction. Approximately 92% effective gas CO + H2 is produced in gasifier R-01.

[0044] A cold water supply line is connected to the bottom of the gasifier R-01. Pipelines No. 14 and No. 17 enter the bottom of the gasifier to cool and wash the syngas. Pipelines No. 12 and No. 9 are connected to the carbon black quench pipe V-02 for further washing of the syngas. Pipeline No. 6 is connected to the carbon black separator V-03. After separation, the gas phase pipeline No. 7 enters the bottom of the scrubbing tower C-01. After separation, the liquid phase pipeline No. 16 is connected to the gasifier R-01. Pipeline No. 15 is connected to the upper part of the scrubbing tower C-01 to wash the syngas and form saturated water gas.

[0045] Syngas scrubbing and cooling process:

[0046] In the combustion chamber of gasifier R-01, the high-temperature syngas at the top of the quench tube is pressurized by washing water pump P-05 via pipeline 14. After flow regulation by FV-14, it enters the quench ring for preliminary washing and cooling of the syngas. The syngas then enters the quench chamber water bath through the downcomer. The bottom of the quench chamber is connected to pipeline 17, and after flow regulation by FV-17, it enters the quench chamber, maintaining the liquid level to form a water bath. After exiting the quench chamber, the syngas connects to the top of the carbon black quench tube via pipeline 5. The upper part of the carbon black quench tube is connected to pipeline 12, and the quench water flow rate is regulated by FV-12. Pipeline 9 is connected to the lower part of the carbon black quench tube V-02, and is pressurized by spray water pump P-03 and regulated by spray water pump FV-09. The synthesis gas is washed by quench water, spray water, and quenching water in the carbon black quench tube V-02. After preliminary washing, the synthesis gas enters the carbon black separator V-03 through pipeline No. 6. The carbon black separator V-03 separates the free water in the synthesis gas. The gas phase enters the bottom of the scrubbing tower C-01 through pipeline No. 7, and the liquid phase goes to the gasifier through pipeline No. 16. In the scrubbing tower V-03, the synthesis gas is thoroughly washed from bottom to top by the scrubbing water from pipeline No. 15 at the outlet of the scrubbing water pump P-05. The pressure in the boundary area is controlled by PV-01 through pipeline No. 8 at the outlet of the scrubbing tower V-03, thereby controlling the reaction residence time in the gasifier, ensuring gasification efficiency, low ash content in phenol tar, low scrubbing water volume, and saving power consumption and water treatment costs.

[0047] The feeding process of this invention system is as follows:

[0048] The feed oil buffer tank V-01 is pressurized via pipeline 21. PV-21 is opened to pressurize feed oil buffer tank V-01. On pipeline 22, PV-22 is opened to depressurize and replace feed oil buffer tank V-01. The pressure of feed oil buffer tank V-01 is controlled at 0.7 MPa. Pipeline 1 is the EST oil residue feed line. EST oil residue is added to feed oil buffer tank V-01 by adjusting the flow rate via FV-01. Pipeline 2 is the vacuum residue oil line. Vacuum residue oil is added to feed oil buffer tank V-01 by adjusting the flow rate via FV-02. Phenol tar is pressurized in phenol tar buffer tank V-04 via phenol tar P-07. The phenol tar feed pressure is adjusted to 1.0 MPa via PV-20. Shut-off valve 2 is opened, and the flow rate changes via FV-01, adjusting the ratio of phenol tar to EST oil residue.

[0049] Pipeline No. 4 is the feed oil pipeline. The feed oil is pressurized by the feed oil pump P-02, which is also a variable frequency pump. The flow rate is adjusted by frequency conversion. The oxygen flow rate is adjusted by FV-03 in pipeline No. 3. The oxygen-oil ratio is controlled. Precise oxygen-oil ratio control is the key to the safe operation of gasifier R-01 and an important means to control the gasification reaction efficiency.

[0050] Pipelines No. 3 and No. 4 enter gasifier R-01, where an incomplete oxidation reaction occurs. It is calculated that the carbon conversion rate of the gasification reaction reaches 98%, producing approximately 95% effective gas CO+H2.

[0051]

[0052]

[0053]

[0054]

[0055] Therefore, it can be seen that the ability to recycle waste materials can reduce water and energy consumption, increase product quality, and has broad market application prospects.

[0056] Finally, it should be noted that the present invention is not limited to the above embodiments, and many variations are possible. All variations that can be directly derived or conceived by those skilled in the art from the disclosure of the present invention should be considered within the scope of protection of the present invention.

Claims

1. A system for producing green hydrogen from phenol tar, characterized in that: It includes feed oil buffer tank (V-01), phenol acetone tar buffer tank (V-04), the phenol acetone tar buffer tank (V-04) is connected with No. 19 pipeline, No. 18 pipeline by phenol acetone tar feed pump (P-07) respectively, the feed oil buffer tank (V-01) side is equipped with No. 1 pipeline, No. 2 pipeline, No. 19 pipeline, No. 18 pipeline is connected on No. 1 pipeline, No. 2 pipeline respectively, the feed oil buffer tank (V-01) bottom is connected with feed oil circulating pump (P-01) by No. 23 pipeline, and the feed oil circulating pump (P-01) is connected with feed oil pump (P-02) by No. 23 pipeline, after pressurization by feed oil pump (P-02) by No. 4 pipeline is connected in the process burner on the top of gasification furnace (R-01), the quenching chamber in the gasification furnace (R-01) is connected in the top of carbon black quenching pipe (V-02) by No. 5 pipeline, the bottom of carbon black quenching pipe (V-02) is connected with carbon black separator (V-03) by No. 6 pipeline, the top of carbon black separator (V-03) is connected in the lower part of washing tower (C-01) by No. 7 pipeline, the bottom of carbon black separator (V-03) is connected to the gasification furnace (R-01) by No. 17 pipeline with black water pump (P-04), the upper part of carbon black quenching pipe (V-02) is connected with No. 12 pipeline with quenching water flow regulating valve (FV-12), the bottom of washing tower (C-01) is connected with quenching water pump (P-06), the quenching water pump (P-06) is communicated with No. 12 pipeline, and the quenching water pump (P-06) is gathered after No. 12 pipeline by No. 11 pipeline is connected on the upper part of washing tower (C-01) for spraying, still includes washing water pump (P-05), the washing water pump (P-05) is connected on the gasification furnace (R-01) by No. 14 pipeline and is connected on the upper part of washing tower (C-01) by No. 15 pipeline, the top of washing tower (C-01) is connected with methanol washing tower (C-02) by No. 8 pipeline, the No. 8 pipeline controls gasification system pressure simultaneously and sends synthesis gas to shift converter (R-02) to convert CO in synthesis gas into H2, and then hydrogen is sent into methanol washing tower (C-02) to remove sulfur and carbon, after transformation, purification and purification, pure hydrogen is obtained from synthesis gas; The burner on the top of the gasification furnace (R-01) is also connected with No. 3 pipeline with oxygen flow regulating valve (FV-03), and enters the gasification furnace (R-01) through the process burner, and No. 3 pipeline and No. 4 pipeline control the proportion of entering the process burner of the gasification furnace (R-01), and react in the gasification furnace (R-01); The carbon black quenching pipe (V-02) is connected with spray water pump (P-03) by No. 9 pipeline with spray water flow regulating valve (FV-09);The No. 23 pipeline and the feed oil buffer tank (V-01) are connected with regulating valve (FV-24);The flow proportion of No. 4 pipeline and No. 3 pipeline is controlled, and the mass ratio is controlled at 0.9-1.

3. The combustion chamber of the gasification furnace guides the synthesis gas into the water bath of the quenching chamber through the downcomer, the top of the downcomer is provided with a quenching ring, the quenching water is sprayed at an angle, the No. 14 pipeline is connected to the quenching ring, and the quenching ring is provided with a riser pipe, so that the synthesis gas is fully contacted with the water bath of the quenching chamber and the water carried by the synthesis gas is reduced; the synthesis gas in the quenching chamber passes through the riser pipe to the top of the quenching chamber, and the spray water is arranged at the outlet of the synthesis gas and is provided with a spray water distribution device, after being wetted by the spray water, the synthesis gas is sent out of the gasification furnace through the No. 5 pipeline.

2. The system for producing green hydrogen from phenol tar according to claim 1, characterized in that: The No. 1 pipeline, the No. 23 pipeline and the No. 4 pipeline are provided with patch heating, and the temperature of the patch heating is not less than 220 DEG C, so as to ensure the flowability of the raw materials and the medium temperature for two hours after the heating steam is stopped.

3. The system for producing green hydrogen from phenol tar according to claim 1, characterized in that: The No. 1 pipeline is provided with a slurry valve to ensure that the valve has no dead zone and the high-viscosity oil does not block; the No. 1 pipeline and the No. 2 pipeline are respectively connected with an EST oil residue regulating valve (FV-01) and a vacuum residue flow regulating valve (FV-02).

4. The system for producing green hydrogen from phenol tar according to claim 1, characterized in that: The No. 19 pipeline and the No. 18 pipeline are connected with the No. 20 pipeline provided with a phenol acetone pressure regulating valve (PV-20), and the No. 20 pipeline is a reflux line which is connected to a phenol acetone tar buffer tank (V-04) to regulate the phenol tar supply pressure and ensure that the phenol tar is smoothly added to the EST oil residue.

5. The system for producing green hydrogen from phenol tar according to claim 1, characterized in that: The No. 2 pipeline transports the vacuum residue, the No. 18 pipeline is adjusted and added to the No. 2 pipeline through a stop valve 1, the No. 19 pipeline is added to the No. 1 pipeline in proportion through a stop valve 2, and the pressure is adjusted and added through the No. 20 pipeline.

6. The system for producing green hydrogen from phenol tar according to claim 1, characterized in that: The feed oil buffer tank (V-01) is connected with a No. 21 pipeline and a No. 22 pipeline, the No. 21 pipeline is connected with a feed oil buffer tank pressure charging valve (PV-21) to realize medium-pressure nitrogen charging, and the No. 22 pipeline is connected with a feed oil buffer tank pressure relief valve (PV-22) to realize pressure relief, the pressure of the feed oil buffer tank (V-01) is controlled at 0.7 MPa, the inlet flow rate of a feed oil circulating pump (P-01) is ensured, and pipeline blockage is avoided.

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