System for converting high-metal high-sulfur heavy dirty oil into synthesis gas and recovering heavy metals

Abstract

A system for converting high-metal high-sulfur heavy dirty oil into synthesis gas and recovering heavy metals relates to the technical field of petrochemical engineering, and comprises a gasification furnace, the gasification furnace comprises a combustion chamber at the upper part and a chilling chamber at the lower part, and the top of the combustion chamber of the gasification furnace is connected with a No.46 pipeline, a No.1 pipeline and a No.2 pipeline; the upper end of the gasification furnace chilling chamber is connected with the top of the first-stage prewashing tower through a third pipeline, the bottom of the first-stage prewashing tower is connected with the upper end of the separator through a fourth pipeline, the top of the separator is connected with the lower end of the washing tower through a fifth pipeline, and the top of the washing tower is connected with a sixth pipeline; according to the system, hazardous wastes such as oil residues, catalytic slurry oil and phenol-acetone tar and liquid hydrocarbons such as waste heavy dirty oil can be reasonably treated, effective components of the hazardous wastes and the liquid hydrocarbons can be recycled, secondary cost and environmental pollution caused by hazardous waste treatment are avoided, and the market application prospect is wide.

Description

Technical Field

[0001] The invention relates to the technical field of petrochemical engineering, and in particular to a system for converting high-metal and high-sulfur heavy dirty oil into synthesis gas and recovering heavy metals. Background Art

[0002] Liquid hydrocarbons such as oil residue, catalytic oil slurry, phenol acetone tar, etc. are all waste and hazardous waste in the petroleum and chemical industries. They have the common characteristics of high calorific value, high viscosity, high heavy metal and sulfur content, but are difficult to separate and recycle. Traditional use as fuel not only causes energy waste, but also often has low combustion temperature and cannot be completely decomposed, causing environmental pollution.

[0003] Oil residue is the tailings of slurry bed hydrogenation. In order to control the content of metals and solids generated in the slurry reaction unit, a small amount of residual oil is cooled and discharged as oil residue after the reaction. The total amount of Ni, V and Mo in the oil residue is as high as 10000ppm-wt, which is traditionally treated as hazardous waste.

[0004] Catalytic oil slurry, the tailings of catalytic cracking units, has high density, high operating temperature, high content of polycyclic aromatic hydrocarbons and contains a large amount of catalyst dust. It is prone to high-temperature condensation of heavy components to form coking and scaling or deposition and scaling of solid particles, and has the characteristics of high sulfur content.

[0005] Phenol tar is a byproduct of the co-production of phenol and acetone by the cumene process. The composition of phenol tar is complex, mainly containing phenol, acetophenone, 4-cumylphenol, 2,4-diphenyl-4-methyl-1-pentene, 2,4-dicumylphenol, UIRES, m-cresol, p-cresol, 2-phenylpropanal, dimethylbenzyl alcohol, etc. It belongs to HW11 hazardous waste in the hazardous waste catalog, and the separation and recovery energy consumption is high.

[0006] Waste heavy oil is a common waste liquid in the petrochemical field. It has many impurities, high recycling costs, high storage and transportation costs, and complex traditional secondary conversion processes. Summary of the invention

[0007] In view of the above deficiencies in the prior art, the object of the present invention is to provide a system for converting high-metal and high-sulfur heavy waste oil into synthesis gas and recovering heavy metals, which can solve the above technical problems.

[0008] In order to achieve the above object, the present invention provides the following technical solutions: A system for converting high-metal and high-sulfur heavy oil into synthesis gas and recovering heavy metals, comprising a gasifier, the gasifier comprising an upper combustion chamber and a lower quenching chamber, the top of the gasifier combustion chamber is connected to pipeline No. 46, pipeline No. 1 and pipeline No. 2, the upper end of the gasifier quenching chamber is connected to the top of a primary pre-washing tower through pipeline No. 3, the bottom of the primary pre-washing tower is connected to the upper end of a separator through pipeline No. 4, the top of the separator is connected to the lower end of a washing tower through pipeline No. 5, the top of the washing tower is connected to pipeline No. 6, and pipeline No. 44 is connected to pipeline No. 6.

[0009] Preferably, the bottom of the washing tower is connected to pipeline No. 7, pipeline No. 8 and pipeline No. 9 are connected to pipeline No. 7, the other end of pipeline No. 8 is connected to the upper end of the washing tower, the other end of pipeline No. 9 is connected to a heat exchanger, the heat exchanger is connected to a filter through pipeline No. 10, and the filter is connected to the upper end of the first-level pre-washing tower through pipeline No. 11.

[0010] Preferably, pipeline No. 12 is connected to the bottom of the separator, pipeline No. 12 is connected to pipeline No. 13 and pipeline No. 14, the other end of pipeline No. 13 is connected to the first-stage flash concentration tower, and the other end of pipeline No. 14 is connected to the lower end of the gasifier quenching chamber through pipeline No. 15.

[0011] Preferably, a No. 16 pipeline is connected to the bottom of the gasifier quenching chamber, the No. 16 pipeline is connected to the primary flash concentration tower through the No. 17 pipeline, and the primary flash concentration tower is connected to the secondary flash concentration tower through the No. 18 pipeline.

[0012] Preferably, the bottom of the secondary flash concentration tower is connected to the black water storage tank through pipeline No. 19, pipeline No. 45 is connected to the pipeline No. 19, the black water storage tank is connected to the plate and frame filter press through pipeline No. 20, and the plate and frame filter press is connected to the filtrate storage tank through pipeline No. 21.

[0013] Preferably, the lower end of the filtrate storage tank is connected to pipeline No. 22, pipeline No. 22 is connected to pipeline No. 23 and pipeline No. 25, the other end of pipeline No. 23 is respectively connected to the lower end of the first-level pre-wash tower and the lower cone section of the gasifier combustion chamber through pipeline No. 24, the other end of pipeline No. 25 is connected to the heat exchange section of the second-level flash concentration tower, the heat exchange section of the second-level flash concentration tower is connected to the heat exchange section of the first-level flash concentration tower through pipeline No. 26, and the heat exchange section of the first-level flash concentration tower is connected to the hot water storage tank through pipeline No. 27.

[0014] Preferably, pipeline No. 28 is connected to the bottom of the hot water storage tank, pipeline No. 28 is connected to pipeline No. 29, pipeline No. 29 is connected to pipeline No. 30 and pipeline No. 31, the other end of pipeline No. 30 is connected to the upper end of the washing tower, and the other end of pipeline No. 31 is respectively connected to the multi-channel swirl water spray ring of the gasifier and the synthesis gas outlet spray ring of the gasifier.

[0015] Preferably, the plate and frame filter press is connected to the filter cake storage tank through a belt conveyor, the filter cake storage tank is connected to the top of the primary incinerator through pipeline No. 33 via a weighing screw conveyor, the top of the primary incinerator is connected to the top of the fly ash dust collector through pipeline No. 34, the bottom of the fly ash dust collector is connected to the lower end of the primary incinerator through pipeline No. 35, the upper end of the fly ash dust collector is connected to the secondary incinerator through pipeline No. 36, the top of the primary incinerator is connected to pipeline No. 37, the pipeline No. 37 is connected to the secondary incinerator through pipeline No. 38, the lower end of the secondary incinerator is connected to pipeline No. 39, and the bottom of the secondary incinerator is connected to pipeline No. 40.

[0016] Preferably, the bottom of the primary incinerator is connected to pipeline No. 41, pipeline No. 41 is connected to a screener, the screener is connected to a wet separator via pipeline No. 42, and pipeline No. 43 is connected to the wet separator.

[0017] Preferably, pipeline No. 46, pipeline No. 2, pipeline No. 44, pipeline No. 8, pipeline No. 11, pipeline No. 15, pipeline No. 19, pipeline No. 45, pipeline No. 24, pipeline No. 25, pipeline No. 30 and pipeline No. 31 are all provided with flow regulating valves, pipeline No. 1, pipeline No. 7, pipeline No. 14, pipeline No. 20, pipeline No. 23, pipeline No. 25 and pipeline No. 28 are all provided with pressure pumps, pipeline No. 6 is provided with a pressure regulating valve, pipeline No. 13, pipeline No. 16 and pipeline No. 18 are all provided with angle regulating valves, pipeline No. 22 is provided with desalination equipment, and pipeline No. 37 is provided with a fan.

[0018] Compared with the prior art, the beneficial effects of the present invention are as follows: oil residue, catalytic oil slurry, phenol tar and heavy waste oil are used as raw materials to undergo incomplete oxidation reaction with pure oxygen in the gasifier to generate synthesis gas mainly composed of carbon monoxide and hydrogen, the carbon conversion rate of the gasifier reaches more than 98%, and the production wastewater meets the environmental protection indicators; the filter cake after combustion in the gasifier enters the metal recovery device and is incinerated twice to obtain metal ash, and the metal ash is wet-sorted to obtain high-value-added high-purity metal. Through this system, hazardous wastes such as oil residue, catalytic oil slurry, phenol acetone tar are harmlessly treated, and waste heavy waste oil is recovered, converted and utilized, avoiding environmental pollution and making effective and reasonable use of energy. BRIEF DESCRIPTION OF THE DRAWINGS

[0019] In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings required for use in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments recorded in the present invention. For ordinary technicians in this field, other drawings can also be obtained based on these drawings.

[0020] Figure 1 It is a schematic diagram of the process of the present invention.

[0021] Description of reference numerals: 1-Pipeline 1, 2-Pipeline 2, 3-Pipeline 3, 4-Pipeline 4, 5-Pipeline 5, 6-Pipeline 6, 7-Pipeline 7, 8-Pipeline 8, 9-Pipeline 9, 10-Pipeline 10, 11-Pipeline 11, 12-Pipeline 12, 13-Pipeline 13, 14-Pipeline 14, 15-Pipeline 15, 16-Pipeline 16, 17-Pipeline 17, 18-Pipeline 18, 19-Pipeline 19, 20-Pipeline 20, 21-Pipeline 21 , 22-Pipeline No. 22, 23-Pipeline No. 23, 24-Pipeline No. 24, 25-Pipeline No. 25, 26-Pipeline No. 26, 27-Pipeline No. 27, 28-Pipeline No. 28, 29-Pipeline No. 29, 30-Pipeline No. 30, 31-Pipeline No. 31, 32-Belt Conveyor, 33-Pipeline No. 33, 34-Pipeline No. 34, 35-Pipeline No. 35, 36-Pipeline No. 36, 37-Pipeline No. 37, 38-Pipeline No. 38, 3 9-Pipeline No. 39, 40-Pipeline No. 40, 41-Pipeline No. 41, 42-Pipeline No. 42, 43-Pipeline No. 43, 44-Pipeline No. 44, 45-Pipeline No. 45, 46-Pipeline No. 46, 47-Gasifier, 48-First-level pre-wash tower, 49-Separator, 50-Washing tower, 51-Heat exchanger, 52-Filter, 53-First-level flash concentration tower, 54-Second-level flash concentration tower, 55-Black water storage tank, 56-Plate and frame filter press, 57-Filtrate storage tank, 58-hot water storage tank, 59-filter cake storage tank, 60-weighing screw conveyor, 61-primary incinerator, 62-fly ash dust collector, 63-secondary incinerator, 64-screener, 65-wet separator, 66-desalting equipment, 67-fan, 68-visual fire detection, 69-shut-off valve, 70-chimney, 100-furnace air duct, 101-fuel gas duct, 102-flue gas duct, 103-extraction medium duct, 104-duct one, 105-duct two, 106-duct three. DETAILED DESCRIPTION

[0022] The following is a detailed description of the invention by way of examples in conjunction with the accompanying drawings. Obviously, the described embodiments are only a part of the embodiments of the invention, rather than all of the embodiments. Example

[0023] like Figure 1 As shown, the present invention discloses a system for converting high-metal and high-sulfur heavy oil into synthesis gas and recovering heavy metals, including a gasifier 47, the gasifier 47 includes an upper combustion chamber and a lower quenching chamber, the top of the combustion chamber of the gasifier 47 is connected to the No. 46 pipeline 46, the No. 1 pipeline 1 and the No. 2 pipeline 2, the No. 46 pipeline 46 is connected to the ultra-high pressure steam supply system upstream, and the flow is adjusted by the flow regulating valve to be sent to the integrated combination nozzle of the gasifier 47; the No. 1 pipeline 1 is connected to the oil residue, catalytic oil slurry, phenol acetone tar and waste heavy oil feeding system upstream, and is pressurized by a booster pump and sent to the integrated combination nozzle of the gasifier 47; the No. 2 pipeline 2 is connected to the high-pressure oxygen supply system upstream, and the flow is adjusted by the flow regulating valve to be sent to the integrated combination nozzle of the gasifier 47; The regulating valve adjusts the flow rate and then sends it to the integrated combination nozzle of the gasifier 47; the upper end of the quenching chamber of the gasifier 47 is connected to the top of the first-level pre-washing tower 48 through the No. 3 pipeline 3, and the bottom of the first-level pre-washing tower 48 is connected to the upper end of the separator 49 through the No. 4 pipeline 4, and the top of the separator 49 is connected to the lower end of the washing tower 50 through the No. 5 pipeline 5 for secondary washing, and the top of the washing tower 50 is connected to the No. 6 pipeline 6, and the No. 6 pipeline 6 is sent to the conversion, desulfurization and decarbonization system after the pressure is controlled by the pressure regulating valve; the No. 44 pipeline 44 is connected to the No. 6 pipeline 6, and the No. 44 pipeline 44 is superheated steam, which is merged into the No. 6 pipeline 6 through the flow regulating valve to adjust the water-gas ratio of the synthesis gas to ensure the conversion rate of the conversion reaction.

[0024] The bottom of the washing tower 50 is connected to the No. 7 pipeline 7, and the No. 8 pipeline 8 and the No. 9 pipeline 9 are connected to the No. 7 pipeline 7. The other end of the No. 8 pipeline 8 is connected to the upper end of the washing tower 50, and the other end of the No. 9 pipeline 9 is connected to the heat exchanger 51. The heat exchanger 51 is connected to the filter 52 through the No. 10 pipeline 10, and the filter 52 is connected to the upper end of the primary pre-washing tower 48 through the No. 11 pipeline 11. After being pressurized by the booster pump, the No. 7 pipeline 7 is divided into two routes: one route is used as washing water after the flow rate is adjusted by the No. 8 pipeline 8 through the flow regulating valve to the washing tower 50; the other route is used as washing water after the heat exchange of the No. 9 pipeline 9 through the No. 10 pipeline 10 to the filter 52 to prevent clogging of the multi-channel swirl water spray ring of the gasifier 47; the No. 11 pipeline 11 is used as washing water from the filter 52 through the flow regulating valve to the upper part of the primary pre-washing tower 48 to perform primary washing of the synthesis gas.

[0025] The bottom of the separator 49 is connected to the No. 12 pipeline 12, and the No. 13 pipeline 13 and the No. 14 pipeline 14 are connected to the No. 12 pipeline 12. The other end of the No. 13 pipeline 13 is connected to the first-stage flash concentration tower 53, and the other end of the No. 14 pipeline 14 is connected to the lower end of the quenching chamber of the gasifier 47 through the No. 15 pipeline 15. The No. 12 pipeline 12 is divided into two routes from the bottom of the separator 49: one route, the No. 13 pipeline 13, is regulated by an angle regulating valve to the first-stage flash concentration tower 53 for flash concentration and heat recovery, and the other route, the No. 14 pipeline 14, is pressurized by a pressure pump to the No. 15 pipeline 15, and the No. 15 pipeline 15 is sent to the bottom of the quenching chamber of the gasifier 47 after passing through a flow regulating valve to maintain the circulation flow at the bottom of the quenching chamber to prevent ash from being deposited at the bottom of the quenching chamber of the gasifier 47.

[0026] The bottom of the quenching chamber of the gasifier 47 is connected to the No. 16 pipeline. The No. 16 pipeline is regulated by an angle regulating valve and sent to the first-level flash concentration tower 53 through the No. 17 pipeline 17 for flash concentration and heat recovery. The black water in the quenching chamber of the gasifier 47 is discharged quantitatively to maintain the stability of the liquid level and water quality in the quenching chamber. The first-level flash concentration tower 53 is regulated by an angle regulating valve and reduced in pressure through the No. 18 pipeline 18 and sent to the second-level flash concentration tower 54. The black water undergoes second-level flash concentration and heat recovery.

[0027] The bottom of the secondary flash concentration tower 54 is connected to the black water storage tank 55 through the No. 19 pipeline 19, and the No. 45 pipeline 45 is connected to the No. 19 pipeline 19. The black water storage tank 55 is connected to the plate and frame filter press 56 through the No. 20 pipeline 20, and the plate and frame filter press 56 is connected to the filtrate storage tank 57 through the No. 21 pipeline 21. Pipeline No. 19 flows from the bottom of the secondary flash concentration tower 54 under pressure and is adjusted by a flow regulating valve to the black water storage tank 55. The pressure gravity flow saves electricity and flash breaking measures are set in the pipeline to prevent gas-liquid-solid three-phase flow and avoid rapid wear of the pipeline; Pipeline No. 45 is an alkali liquid line, which is merged into Pipeline No. 19. When the sulfur content of the liquid hydrocarbon raw material entering the gasifier 47 is high, the amount of alkali liquid added is adjusted by the flow regulating valve of Pipeline No. 45 to control the pH of the black water system and prevent acid corrosion; Pipeline No. 20 flows from the black water storage tank 55 to the plate and frame filter press 56 for solid-liquid separation; Pipeline No. 21 flows from the clear liquid of the plate and frame filter press 56 to the filtrate storage tank 57.

[0028] The lower end of the filtrate storage tank 57 is connected to pipeline No. 22, and a desalting device 66 is arranged on pipeline No. 22. Pipeline No. 23 and pipeline No. 25 are connected to pipeline No. 22. The other end of pipeline No. 23 is respectively connected to the lower end of the first-level pre-washing tower 48 and the lower cone section of the combustion chamber of the gasifier 47 through pipeline No. 24. The other end of pipeline No. 25 is connected to the heat exchange section of the second-level flash concentration tower 54. The heat exchange section of the second-level flash concentration tower 54 is connected to the heat exchange section of the first-level flash concentration tower 53 through pipeline No. 26. The heat exchange section of the first-level flash concentration tower 53 is connected to the hot water storage tank 58 through pipeline No. 27. A desalting device 66 is set from the filtrate storage tank 57 of pipeline No. 22. The desalting device 66 removes soluble salt particles in the liquid phase to reduce system scaling. The filtrate after desalting is divided into two routes: one route is pipeline No. 23, which is pressurized by a pressure pump to pipeline No. 24, which passes through flow regulating valves to the lower part of the first-level pre-washing tower 48, and then passes through flow regulating valves to the side of the lower cone plate quenching chamber of the combustion chamber of the gasifier 47 for spray washing to prevent dust accumulation and overheating of the lower cone plate; the other route is pipeline No. 25, which is pressurized by a pressure pump and passes through a flow regulating valve to recover the flash steam heat through the heat exchange section of the second-level flash concentration tower 54 and the heat exchange section of the first-level flash concentration tower 53, and then passes through pipeline No. 27 to the hot water storage tank 58.

[0029] The bottom of the hot water storage tank 58 is connected to the No. 28 pipeline 28, the No. 29 pipeline 29 is connected to the No. 28 pipeline 28, the No. 30 pipeline 30 and the No. 31 pipeline 31 are connected to the No. 29 pipeline 29, the other end of the No. 30 pipeline 30 is connected to the upper end of the washing tower 50, and the other end of the No. 31 pipeline 31 is respectively connected to the multi-channel swirl water spray ring of the gasifier 47 and the synthesis gas outlet spray ring of the gasifier 47. The No. 28 pipeline 28 is pressurized by the pressure pump from the hot water storage tank 58 and is divided into two routes: one route is the No. 30 pipeline 30 and passes through the flow regulating valve to the upper section of the washing tower 50, and the other route is the No. 31 pipeline 31 and passes through the flow regulating valve to the multi-channel swirl water spray ring of the gasifier 47 and the synthesis gas outlet spray ring of the gasifier 47.

[0030] The plate and frame filter press 56 is connected to the filter cake storage tank 59 through the belt conveyor 32, the filter cake storage tank 59 is connected to the top of the primary incinerator 61 through the No. 33 pipeline 33 via the weighing screw conveyor 60, the top of the primary incinerator 61 is connected to the top of the fly ash dust collector 62 through the No. 34 pipeline 34, the bottom of the fly ash dust collector 62 is connected to the lower end of the primary incinerator 61 through the No. 35 pipeline 35, the upper end of the fly ash dust collector 62 is connected to the secondary incinerator 63 through the No. 36 pipeline 36, the top of the primary incinerator 61 is connected to the No. 37 pipeline 37, the No. 37 pipeline 37 is connected to the secondary incinerator 63 through the No. 38 pipeline 38, the lower end of the secondary incinerator 63 is connected to the No. 39 pipeline 39, and the bottom of the secondary incinerator 63 is connected to the No. 40 pipeline 40. Belt conveyor 32 goes from plate and frame filter press 56 to filter cake storage tank 59; pipeline No. 33 is quantitatively delivered from filter cake storage tank 59 to primary incinerator 61 via weighing screw conveyor 60; pipeline No. 34 is from the top of primary incinerator 61 to fly ash dust collector 62; pipeline No. 35 returns fly ash collected by fly ash dust collector 62 to primary incinerator 61; pipeline No. 36 is from fly ash dust collector 62 to secondary incinerator 63; pipeline No. 37 is from primary incinerator 61 to pipeline No. 38 after pressurization by fan 67 to secondary incinerator 63; pipeline No. 39 is combustion exhaust gas, which is discharged after heat recovery, desulfurization and denitrification meet the standards; pipeline No. 40 transports ash to general solid waste treatment.

[0031] The bottom of the primary incinerator 61 is connected to the No. 41 pipeline, the No. 41 pipeline is connected to the screener 64, the screener 64 is connected to the No. 42 pipeline 42, the wet separator 65 is connected to the No. 43 pipeline, and the No. 43 pipeline leads to storage and transportation packaging.

[0032] Furthermore, in this embodiment, the pipeline No. 1 is provided with patch heating, which ensures that the heating temperature is not lower than 220°C, ensures the fluidity of the raw materials, and ensures the medium temperature for two hours after the heating steam is stopped. The pipeline No. 1 is provided with a slurry valve to ensure that the valve has no dead zone and the high-viscosity crude oil is not blocked.

[0033] The No. 46 pipeline 46 is provided with a flow regulating valve to adjust the steam flow into the gasifier 47. The No. 2 pipeline 2 is provided with a flow regulating valve to adjust the oxygen flow into the gasifier 47. The No. 1 pipeline 1 adjusts the feed oil flow through the frequency conversion of the pressure pump. The steam flow, oxygen flow and feed oil flow are strictly proportionally controlled, and the methane composition in the synthesis gas is used as the control target to form an automatic control loop and is provided with a protection interlock. The mass ratio is controlled at 0.9~1.3.

[0034] The pipeline No. 46, pipeline No. 1 and pipeline No. 2 enter the gasifier 47, and an incomplete oxidation reaction occurs in the gasifier 47. The reaction pressure is 4.0MPa~8.6MPa, and the temperature is controlled at 1100℃~1600℃. Pipeline No. 1 and pipeline No. 2 are the main reactions, and about 92% of effective gas (CO+H2) is produced in the gasifier 47.

[0035] A cold water replenishment pipeline is connected to the bottom of the gasifier 47, and the No. 15 pipeline 15 enters the bottom of the gasifier 47 to perform preliminary cooling and washing of the synthesis gas; the No. 31 pipeline 31 passes through a flow regulating valve to the multi-channel swirl water spray ring of the gasifier 47 to cool and wash the high-temperature synthesis gas, and passes through a flow regulating valve to the synthesis gas outlet of the gasifier 47 to spray and flush the synthesis gas pipe mouth; to ensure the quenching effect, two channels are set: the first channel swirls along the inner wall of the downcomer to form a downcomer protective water film with a swirl angle of 5°~30°; the second channel sprays along the vertical direction of 30°~45° obliquely toward the center of the downcomer to fully cool and wash the high-temperature synthesis gas.

[0036] The synthesis gas enters the water bath of the quenching chamber through the downcomer. An ascending pipe is arranged outside the downcomer. After being washed and cooled in the water bath, the high-temperature synthesis gas enters the upper part of the quenching chamber along the gap between the downcomer and the ascending pipe, and a steam baffle is arranged on the ascending pipe and other parts to separate free water. A swirl balance hole is arranged below the liquid level of the water bath of the ascending pipe, and the swirl angle is 5°~60°. The swirl angle can pass part of the synthesis gas to avoid the flow area of ​​the downcomer and the ascending pipe being reduced due to blockage, and serious water carrying. The swirl balance hole is the key to stabilizing the liquid level of the quenching chamber. The bottom of the quenching chamber is connected to the fifteenth pipeline 15. After the flow is adjusted by the flow regulating valve, it enters the quenching chamber to keep the liquid level stable and form a water bath. After the synthesis gas leaves the quenching chamber, it is connected to the top of the primary pre-washing tower 48 through the third pipeline 3.

[0037] A baffle is set at the syngas outlet connection of gasifier 47 to separate free liquid droplets and dust entrained in the syngas leaving the quenching chamber. The bottom of the baffle is hollow to prevent dust and liquid accumulation. The flow rate of pipeline No. 31 is adjusted through a flow regulating valve to the syngas outlet of gasifier 47 for spraying, flushing the syngas pipe opening and flushing the entrained ash into the quenching chamber.

[0038] The upper part of the primary pre-wash tower 48 is connected to the eleventh pipeline 11, and the washing water flow is adjusted by the flow regulating valve. The twenty-fourth pipeline 24 is connected to the lower part of the primary pre-wash tower 48, and the spray water is adjusted by the pressure pump to pressurize the flow regulating valve. The spray water pre-washes the synthesis gas in the primary pre-wash tower 48. The spray water inside the primary pre-wash tower 48 is provided with a shower-type spray head, and the spray angle is 15°~75° to ensure the washing effect of the synthesis gas. The other route of the twenty-fourth pipeline 24 passes through the flow regulating valve and is evenly sprayed to the side of the lower cone plate quenching chamber of the combustion chamber of the gasifier 47, and the connection angle between the cone plate and the quenching chamber is washed to prevent the lower cone plate from ash accumulation and overheating.

[0039] The No. 4 pipeline 4 is connected to the separator 49, and the separator 49 separates free water and carbon black in the synthesis gas. After separation, the gas phase enters the bottom of the washing tower 50 through the No. 5 pipeline 5, and contacts with the washing water from top to bottom in the washing tower 50 from bottom to top in reverse, so as to perform secondary washing on the synthesis gas. The No. 6 pipeline 6 at the outlet of the washing tower 50 is sent to the boundary area, and the pressure is controlled by the pressure regulating valve. The washing tower 50 is a high-efficiency washing tower combined with a tray and a filler, and the ash removal efficiency reaches 99%, and the dust content of the outlet synthesis gas is less than 2PPm; after separation by the separator 49, the liquid phase is connected to the gasifier 47 through the No. 14 pipeline 14, and the conical bottom flow of the quenching chamber of the gasifier 47 is maintained to prevent carbon black deposition; the No. 13 pipeline 13 is connected to the first-level flash concentration tower 53 for first-level flash concentration, and heat is recovered in the top heat exchange section; the No. 8 pipeline 8 and the No. 30 pipeline 30 are connected to the upper part of the washing tower 50 to wash the synthesis gas and form saturated synthesis gas.

[0040] The No. 44 pipeline 44 is superheated steam, which is merged into the No. 6 pipeline 6 to adjust the water-gas ratio of the synthesis gas to ensure the conversion rate of the shift reaction.

[0041] The black water No. 16 pipeline 16 at the bottom of the gasifier 47 quenching chamber is regulated by an angle regulating valve to the first-level flash concentration tower 53 for concentration and heat recovery. A part of the black water at the bottom of the separator 49 enters the gasifier 47 quenching chamber through the No. 14 pipeline 14, and the other part of the black water is regulated by the No. 13 pipeline 13 and sent to the first-level flash concentration tower 53. After the black water in the quenching chamber of the gasifier 47 and the separator 49 is concentrated and heat is recovered, it flows by pressure at the bottom of the first-level flash concentration tower 53 to the second-level flash concentration tower 54 for secondary concentration and heat recovery. The first and second-level flash concentration towers adopt cyclone separation and flash concentration integrated equipment, and have efficient dust removal and heat recovery functions. The wear-resistant and anti-blocking design is fully considered to ensure the cleanliness of flash steam, the concentration of black water and the full recovery of heat.

[0042] The secondary flash concentration tower 54 is connected to the No. 19 pipeline 19 and flows to the black water storage tank 55 through pressure. The pressure self-flow saves electricity and the pipeline is provided with flash evaporation measures to prevent gas-liquid-solid three-phase flow and avoid rapid wear of the pipeline; the black water in the black water storage tank 55 does not need to be settled and an agitator is provided. Considering the oily characteristics of heavy oil carbon black, no flocculant facilities are added to the black water. An aeration coil is set at the bottom of the black water storage tank 55 to prevent bottom dead corner sedimentation, and a side-entry agitator with an inclination angle of 10°~30° is set on the side. The black water in the tank forms a vortex to ensure uniform suspension. A nitrogen seal is set on the top to ensure inertness and corrosion prevention. The No. 45 pipeline 45 is an alkali liquid line, which is merged into the No. 19 pipeline 19. When the sulfur content of the liquid hydrocarbon feedstock entering the gasifier 47 is high, the amount of alkali liquid added is adjusted through the No. 45 pipeline 45 flow regulating valve to control the pH of the black water system to prevent acid corrosion. The concentrated black water from the gasifier 47 does not need to be settled, and is sent to the plate and frame filter press 56 for separation after being pressurized by a pressure pump.

[0043] The plate and frame filter press 56 is connected to the liquid phase pipeline No. 21 21 to collect and recycle the filtrate; the pipeline No. 22 22 is provided with a desalting device 66 from the filtrate storage tank 57, and the desalting device 66 removes soluble salt particles in the liquid phase to reduce system scaling. The filtrate after desalination is respectively sent to the first-level pre-washing tower 48 and the lower cone section of the gasifier 47 through a pressure pump to wash the synthesis gas and spray for cooling; and is sent to the heat exchange section of the second-level flash concentration tower 54 and the heat exchange section of the first-level flash concentration tower 53 through a pressure pump to recover the heat of the flash steam, and then preheated to the hot water storage tank 58.

[0044] The hot water storage tank 58 is connected to pipeline No. 28 28 and is pressurized by a pressure pump to pipeline No. 29 29. Pipeline No. 29 is divided into two routes: one is sent to the upper part of the washing tower 50 through pipeline No. 30 to wash the synthesis gas, and the ash content of the sent synthesis gas is ≤2PPm; the other is sent to the multi-channel swirl water spray ring of the gasifier 47 through pipeline No. 31 to cool and wash the high-temperature synthesis gas, and to the synthesis gas outlet of the gasifier 47 for spraying, and the synthesis gas pipe mouth is flushed.

[0045] The plate and frame filter press 56 is connected to the belt conveyor 32 to deliver the filter cake to the filter cake storage tank 59. The pipeline No. 33 is connected to the weighing screw conveyor 60, and is delivered to the primary incinerator 61 after weighing. The primary incinerator 61 removes the residual carbon in the filter cake. The fly ash dust collector 62 is connected to the pipeline No. 34 34 and the pipeline No. 35 35 to return the captured fly ash to the primary incinerator 61 for further incineration. The fly ash dust collector 62 is connected to the pipeline No. 36 36 to the secondary incinerator 63 for further incineration and heat recovery before being delivered to the desulfurization and denitrification.

[0046] The primary incinerator 61 is connected to pipeline No. 37 37 to fan 67, the fan 67 is connected to pipeline No. 38 38 to the secondary incinerator 63, the secondary incinerator 63 is connected to pipeline No. 39 39 to recover flue gas heat, desulfurize and denitrify to qualified emissions, and the secondary incinerator 63 is connected to pipeline No. 40 40 to ordinary solid waste treatment.

[0047] The primary incinerator 61 is connected to the No. 41 pipeline 41 to the metal ash sifter 64; the wet separator 65 is connected to the No. 42 pipeline 42 to perform wet separation and purification on the metal ash; the wet separator 65 is connected to the No. 43 pipeline 43 to packaging and external transportation. Incineration and wet refining are combined to recover heavy metals, and the heavy metals in the filter cake are recovered with high purity, and the fly ash is converted into ordinary solid waste. The flue gas is discharged after heat recovery, desulfurization and decarbonization, avoiding environmental pollution, increasing benefits, and reducing processing costs.

[0048] Feeding system process of the present invention: Pipeline No. 46 is a steam pipeline, which is equipped with a flow regulating valve to adjust the steam flow into the gasifier 47; Pipeline No. 1 is a feed oil pipeline, which transports liquid hydrocarbons such as oil residue, catalytic oil slurry, phenol acetone tar and waste heavy oil, and the flow is adjusted by frequency conversion of the booster pump; Pipeline No. 2 is a high-pressure oxygen pipeline, which is equipped with a flow regulating valve to adjust the oxygen flow into the gasifier 47. The steam flow, oxygen flow and feed oil flow are strictly controlled in proportion, and the methane composition in the synthesis gas is used as the control target to form an automatic control loop and set a protection interlock.

[0049] Gasification system process: Pipeline No. 1 is the feed oil pipeline. The feed oil is pressurized by a booster pump. At the same time, the booster pump is a variable frequency pump. The flow rate is adjusted by frequency conversion. Pipeline No. 2 adjusts the flow rate through a flow control valve, which is proportional to the feed oil. Accurate oxygen-oil ratio control is the key to the safe operation of the gasifier 47 and an important means to control the gasification reaction efficiency.

[0050] The No. 46 pipeline 46, No. 1 pipeline 1 and No. 2 pipeline 2 enter the gasifier 47, and an incomplete oxidation reaction occurs in the gasifier 47, with No. 1 pipeline 1 and No. 2 pipeline 2 as the main reactions. The carbon conversion rate of the gasification reaction is calculated to reach 98%, producing about 95% of effective gas (CO+H2).

[0051] The high-temperature synthesis gas in the combustion chamber of the gasifier 47 passes through a multi-channel swirl water spray ring, and the No. 31 pipeline 31 adjusts the flow rate to the multi-channel swirl water spray ring of the gasifier 47 through a flow regulating valve to cool and wash the high-temperature synthesis gas, and adjusts the flow rate to the synthesis gas outlet of the gasifier 47 through a flow regulating valve for spraying, and flushing the synthesis gas pipe mouth; the bottom of the quenching chamber is connected to the No. 15 pipeline 15, and after the flow rate is adjusted by the flow regulating valve, it enters the quenching chamber to keep the liquid level stable to form a stable water bath; after the synthesis gas leaves the quenching chamber, it is connected to the top of the first-level pre-washing tower 48 through the No. 3 pipeline 3, and the upper part of the first-level pre-washing tower 48 is connected to the No. 11 pipeline 11, and the flow rate of washing water is adjusted by the flow regulating valve, and the No. 24 pipeline 24 is connected to the lower part of the first-level pre-washing tower 48, and the flow regulating valve is used to pressurize the pressure pump to adjust the spray water, and the spray water enters the first-level pre-washing tower 48. Pre-washing is carried out, and another route of pipeline No. 24 24 is uniformly sprayed to the side of the lower cone plate quenching chamber of the combustion chamber of the gasifier 47 for washing after the flow is adjusted by a flow regulating valve to prevent dust accumulation and overheating of the lower cone plate; the synthesis gas after preliminary washing enters the separator 49 through pipeline No. 4, and the separator 49 separates free water and carbon black in the synthesis gas, and the gas phase enters the bottom of the washing tower 50 through pipeline No. 5, and the liquid phase is sent to the gasifier 47 through pipeline No. 12. The synthesis gas in the washing tower 50 is fully washed from bottom to top by the washing water from pipeline No. 30 at the outlet of the pressure pump, and the pressure of the washing tower 50 outlet pipeline No. 6 6 is sent to the boundary area and controlled by the pressure regulating valve, thereby controlling the reaction residence time of the gasifier to ensure the gasification efficiency; the superheated steam pipeline No. 44 44 is adjusted by the flow regulating valve and then merged into pipeline No. 6 6 to adjust the water-gas ratio of the synthesis gas to ensure the conversion rate of the shift reaction.

[0052] Black water treatment system process: The black water at the bottom of the quenching chamber of the gasifier 47 is regulated by an angle regulating valve through the No. 16 pipeline 16 and then sent to the primary flash concentration tower 53 for concentration and heat recovery. A part of the black water at the bottom of the separator 49 enters the quenching chamber of the gasifier 47 through the No. 14 pipeline 14, and the other part is sent to the primary flash concentration tower 53 through the No. 13 pipeline 13 after being regulated by an angle regulating valve. After the heat of concentration is recovered, the black water in the quenching chamber of the gasifier 47 and the separator 49 flows by pressure gravity at the bottom of the primary flash concentration tower 53 to the secondary flash concentration tower 54 for secondary concentration and heat recovery.

[0053] After the black water is concentrated by secondary flash evaporation, it is sent to the black water storage tank 55 after being regulated by pipeline No. 19 and flow regulating valve. Alkali solution is added after the flow regulating valve to adjust the low pH value caused by the increased sulfur content of liquid hydrocarbon in the raw material. The black water in the black water storage tank 55 does not need to be settled and is equipped with an agitator. The black water is sent to the plate and frame filter press 56 through a pressure pump. The filtrate after filtration is recycled and the filter cake is sent to metal recovery; the filtrate is recycled through pipeline No. 22 22, and a desalting device 66 is set on pipeline No. 22 22 to purify the recycled water.

[0054] Metal recycling process: The filter cake after filtration by the plate and frame filter press 56 is sent to the filter cake storage tank 59 via the belt conveyor 32, and the pipeline No. 33 is weighed and measured by the weighing screw conveyor 60 and then sent to the primary incinerator 61. The pipeline No. 41 at the bottom of the incinerator is mixed metal ash, which is screened by the sifter 64 and then sent to the wet separator 65 to obtain a single metal for packaging and transportation; the dusty flue gas from the pipeline No. 37 at the top of the primary incinerator 61 is sent to the secondary incinerator 63 via the fan 67. After the secondary combustion, the pipeline No. 39 sends the flue gas to the subsequent heat recovery, desulfurization and denitrification treatment and is discharged into the atmosphere after passing the qualified treatment. The pipeline No. 40 is the secondary incineration ash, which is treated as general solid waste.

[0055] The thirty-fourth pipeline 34 delivers the dust-laden flue gas to the fly ash dust collector 62, the fly ash is returned to the primary incinerator 61 through the thirty-fiveth pipeline 35, and the flue gas is delivered to the secondary incinerator 63 for further combustion.

[0056] Start-up furnace process: The fuel gas pipeline 101 is merged into the No. 1 pipeline 1 and the flow rate is adjusted by a flow regulating valve. The furnace air pipeline 100 is merged into the No. 2 pipeline 2 and the flow rate is adjusted by a flow regulating valve. The flow enters the integrated combination nozzle and the air-fuel ratio and flow rate are accurately controlled by the flow regulating valve to control the combustion load and intensity. The furnace fire detection adopts a visual fire detection 68, which is isolated by a cut-off valve 69 after feeding to protect the visual fire detection 68.

[0057] The flue gas is discharged through the synthesis gas No. 3 pipeline 3 of the quenching chamber of the gasifier 47, extracted by the extractor, and mixed with the extraction medium pipeline 103 and the flue gas pipeline 102, and then discharged to the chimney 70 through the pipeline 104. In order to ensure the residence time of the furnace flue gas and the furnace is fully and stably baked, the liquid level in the quenching chamber of the gasifier 47 is higher than the combustion chamber of the air duct during the baking process, which is a slight positive pressure, and the flue gas breaks through the liquid seal of the quenching chamber and is discharged.

[0058] During furnace drying, the quenching water of the multi-channel swirl water spray ring of the gasifier 47 is supplied by the pressure pump to the pipeline three 106 through the pipeline No. 31 31, and the preheated water of the furnace is discharged to the filtrate storage tank 57 through the pipeline two 105 to establish the quenching water circulation of the furnace to protect the multi-channel swirl water spray ring and the air guide pipe of the gasifier 47.

[0059] The above description is only a preferred specific implementation manner of the present invention, but the protection scope of the present invention is not limited thereto. Any technician familiar with the technical field can make equivalent replacements or changes according to the technical solution and application concept of the present invention within the technical scope disclosed by the present invention, which should be covered by the protection scope of the present invention.

Claims

1. A system for converting high-metal and high-sulfur heavy waste oil into synthesis gas and recovering heavy metals, comprising a gasifier (47), wherein the gasifier (47) comprises an upper combustion chamber and a lower quenching chamber, and is characterized in that: The top of the combustion chamber of the gasifier (47) is connected to pipeline No. 46 (46), pipeline No. 1 (1) and pipeline No. 2 (2); the upper end of the quenching chamber of the gasifier (47) is connected to the top of the first-stage pre-washing tower (48) through pipeline No. 3 (3); the bottom of the first-stage pre-washing tower (48) is connected to the upper end of the separator (49) through pipeline No. 4 (4); the top of the separator (49) is connected to the lower end of the washing tower (50) through pipeline No. 5 (5); the top of the washing tower (50) is connected to pipeline No. 6 (6); and pipeline No. 44 (44) is connected to the pipeline No. 6 (6).

2. A system for converting high-metal and high-sulfur heavy waste oil into synthesis gas and recovering heavy metals as claimed in claim 1, characterized in that: The bottom of the washing tower (50) is connected to a No. 7 pipeline (7), the No. 7 pipeline (7) is connected to a No. 8 pipeline (8) and a No. 9 pipeline (9), the other end of the No. 8 pipeline (8) is connected to the upper end of the washing tower (50), the other end of the No. 9 pipeline (9) is connected to a heat exchanger (51), the heat exchanger (51) is connected to a filter (52) via a No. 10 pipeline (10), and the filter (52) is connected to the upper end of the primary pre-washing tower (48) via a No. 11 pipeline (11).

3. A system for converting high-metal and high-sulfur heavy waste oil into synthesis gas and recovering heavy metals as claimed in claim 2, characterized in that: The bottom of the separator (49) is connected to a No. 12 pipeline (12), and the No. 12 pipeline (12) is connected to a No. 13 pipeline (13) and a No. 14 pipeline (14), the other end of the No. 13 pipeline (13) is connected to a first-stage flash concentration tower (53), and the other end of the No. 14 pipeline (14) is connected to the lower end of the quenching chamber of the gasifier (47) through a No. 15 pipeline (15).

4. A system for converting high-metal and high-sulfur heavy waste oil into synthesis gas and recovering heavy metals as claimed in claim 3, characterized in that: The bottom of the quenching chamber of the gasifier (47) is connected to a No. 16 pipeline (16), the No. 16 pipeline (16) is connected to a primary flash concentration tower (53) via a No. 17 pipeline (17), and the primary flash concentration tower (53) is connected to a secondary flash concentration tower (54) via an No. 18 pipeline (18).

5. A system for converting high-metal and high-sulfur heavy waste oil into synthesis gas and recovering heavy metals as claimed in claim 4, characterized in that: The bottom of the secondary flash concentration tower (54) is connected to a black water storage tank (55) via a No. 19 pipeline (19), and a No. 45 pipeline (45) is connected to the No. 19 pipeline (19). The black water storage tank (55) is connected to a plate and frame filter press (56) via a No. 20 pipeline (20), and the plate and frame filter press (56) is connected to a filtrate storage tank (57) via a No. 21 pipeline (21).

6. A system for converting high-metal and high-sulfur heavy waste oil into synthesis gas and recovering heavy metals as claimed in claim 5, characterized in that: The lower end of the filtrate storage tank (57) is connected to a No. 22 pipeline (22), and the upper end of the No. 22 pipeline (22) is connected to a No. 23 pipeline (23) and a No. 25 pipeline (25). The other end of the No. 23 pipeline (23) is respectively connected to the lower end of the primary pre-wash tower (48) and the lower cone section of the combustion chamber of the gasifier (47) through a No. 24 pipeline (24). The other end of the No. 25 pipeline (25) is connected to the heat exchange section of the secondary flash concentration tower (54). The heat exchange section of the secondary flash concentration tower (54) is connected to the heat exchange section of the primary flash concentration tower (53) through a No. 26 pipeline (26). The heat exchange section of the primary flash concentration tower (53) is connected to the hot water storage tank (58) through a No. 27 pipeline (27).

7. A system for converting high-metal and high-sulfur heavy waste oil into synthesis gas and recovering heavy metals as claimed in claim 6, characterized in that: The bottom of the hot water storage tank (58) is connected to a No. 28 pipeline (28), the top of the No. 28 pipeline (28) is connected to a No. 29 pipeline (29), the top of the No. 29 pipeline (29) is connected to a No. 30 pipeline (30) and a No. 31 pipeline (31), the other end of the No. 30 pipeline (30) is connected to the upper end of the washing tower (50), and the other end of the No. 31 pipeline (31) is respectively connected to a multi-channel swirl water spray ring of a gasifier (47) and a synthesis gas outlet spray ring of a gasifier (47).

8. A system for converting high-metal and high-sulfur heavy waste oil into synthesis gas and recovering heavy metals as claimed in claim 7, characterized in that: The plate and frame filter press (56) is connected to a filter cake storage tank (59) via a belt conveyor (32); the filter cake storage tank (59) is connected to the top of a primary incinerator (61) via a No. 33 pipeline (33) and a weighing screw conveyor (60); the top of the primary incinerator (61) is connected to the top of a fly ash dust collector (62) via a No. 34 pipeline (34); the bottom of the fly ash dust collector (62) is connected to the primary incinerator (61) via a No. 35 pipeline (35). ), the upper end of the fly ash dust collector (62) is connected to the secondary incinerator (63) through the No. 36 pipeline (36), the top of the primary incinerator (61) is connected to the No. 37 pipeline (37), the No. 37 pipeline (37) is connected to the secondary incinerator (63) through the No. 38 pipeline (38), the lower end of the secondary incinerator (63) is connected to the No. 39 pipeline (39), and the bottom of the secondary incinerator (63) is connected to the No. 40 pipeline (40).

9. A system for converting high-metal and high-sulfur heavy waste oil into synthesis gas and recovering heavy metals as claimed in claim 8, characterized in that: The bottom of the primary incinerator (61) is connected to a No. 41 pipeline (41), the No. 41 pipeline (41) is connected to a screener (64), the screener (64) is connected to a wet separator (65) via a No. 42 pipeline (42), and the wet separator (65) is connected to a No. 43 pipeline (43).

10. A system for converting high-metal and high-sulfur heavy waste oil into synthesis gas and recovering heavy metals as claimed in claim 9, characterized in that: The pipeline No. 46 (46), pipeline No. 2 (2), pipeline No. 44 (44), pipeline No. 8 (8), pipeline No. 11 (11), pipeline No. 15 (15), pipeline No. 19 (19), pipeline No. 45 (45), pipeline No. 24 (24), pipeline No. 25 (25), pipeline No. 30 (30) and pipeline No. 31 (31) are all provided with flow regulating valves. The pipeline No. 1 (1), pipeline No. 7 (7), pipeline No. 14 (1 4), pipeline No. 20 (20), pipeline No. 23 (23), pipeline No. 25 (25) and pipeline No. 28 (28) are all provided with booster pumps, pipeline No. 6 (6) is provided with a pressure regulating valve, pipeline No. 13 (13), pipeline No. 16 (16) and pipeline No. 18 (18) are all provided with angle regulating valves, pipeline No. 22 (22) is provided with a desalination device (66), and pipeline No. 37 (37) is provided with a fan (67).

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