A recovery method for recovering deuterium from deuterium-containing organic waste liquid

Abstract

The application discloses a recovery method for recovering deuterium from deuterium-containing organic waste liquid, and steps are as follows: igniting after adjusting the incinerator to a negative pressure state; after ignition, mixing inert gas as atomization medium, pure oxygen as combustion-supporting gas and deuterium-containing organic waste liquid as incineration object through an atomization burner to form atomized gas-liquid spray for spraying into the incinerator; generating flue gas containing carbon dioxide and deuterium-containing water after the atomized gas-liquid is fully incinerated in the incinerator; cooling the flue gas by using a cooling water in a first heat exchanger and recovering deuterium-containing water in the flue gas; cooling the cooled flue gas again by using chilled water in a second heat exchanger and continuously recovering deuterium-containing water in the flue gas; discharging all tail gas in a tail gas discharge pipe or discharging part of the tail gas and taking the other part of the tail gas as circulating gas for supplying the atomization medium in step B. The recovery method provided by the application can fully incinerate the deuterium-containing organic waste liquid, has no waste residue and harmful gas emission, and realizes that the deuterium recovery rate reaches more than 99.0%.

Description

TECHNICAL FIELD

[0001] The present application belongs to the field of chemical technology, and particularly relates to treatment of organic waste liquid generated in a chemical project, in particular to a recovery method for recovering deuterium from deuterium-containing organic waste liquid. BACKGROUND

[0002] High-concentration organic waste liquid generated in a large chemical project has the characteristics of complex chemical composition, large production load fluctuation, high organic matter content, high harmful element content, flammability, explosiveness, corrosiveness, toxicity, reactivity, etc. To recover elemental substances from the organic waste liquid, a common method for treating organic waste liquid by incineration is a method for recovering elements while treating organic waste liquid.

[0003] Among common methods for treating organic waste liquid, incineration is an extremely effective method. For such high-concentration organic waste liquid, centralized treatment by an incinerator after pretreatment is the current mainstream process, which has the characteristics of small scale, low investment cost, etc., and is widely applied. CN112944371B discloses a harmless treatment method and treatment equipment for organic waste liquid, which mainly includes three processes of organic waste liquid pressurized atomization, organic waste liquid incineration, and tail gas discharge. The organic waste liquid in the waste liquid storage tank is directly atomized and sprayed out by increasing a pump or is sucked to an atomizing nozzle by high-speed compressed air, fully mixed with excess air from a combustion air fan, incinerated, the temperature in the incinerator is above 1100℃, the organic components in the organic waste liquid are completely incinerated, and then the organic waste liquid is cooled to below 200℃ by atomizing cooling water of a tail gas cooling and venting system and then discharged into the atmosphere.

[0004] The main components of deuterium-containing organic waste liquid are deuterated aromatic hydrocarbons with a deuterium substitution degree of 30% or less and deuterated alcohols, and the incineration products are carbon dioxide and low-deuterium water. If the traditional organic waste liquid incineration treatment method is used to recover deuterium elements from deuterium-containing organic waste liquid, the following problems exist:

[0005] (1) The large amount of air sent by the air blower as combustion-supporting gas, the heavy water recovery rate of the organic waste liquid incineration is extremely low, and it cannot be effectively recovered. Taking low-deuterium benzene organic waste liquid as an example: C6H6+7.5O2→6CO2+3H2O, in order to ensure the complete incineration of 1 mol of benzene, oxygen needs to be excessive, if not, 6 mol of carbon dioxide non-condensable gas will be generated after incineration; if air is used as combustion-supporting gas, the oxygen content in air is 21%, at least 35.7 mol of air is needed, and 34.2 mol of non-condensable gas needs to be discharged from the system after incineration, the non-condensable gas discharged from the system is significantly increased, the more non-condensable gas, the more water vapor taken away; if air is used as dispersion gas, the oxygen content is 21%, there is a certain safety risk; in addition, air contains about 80% of nitrogen, if it is converted into acid gas, it will cause corrosion to the equipment; in addition, if air is used as combustion-supporting gas, in order to ensure the complete incineration of organic waste liquid, the flow rate of air needs to be 5 times that of pure oxygen, under the same temperature and pressure, the greater the flow rate, the more water vapor taken away, and the lower the deuterium recovery rate.

[0006] (2) The incineration may produce acid gas under high temperature conditions, which may cause corrosion to the equipment. If air is introduced into the incineration system, whether as combustion-supporting gas or dispersion gas, nitrogen in air is oxidized to generate nitric oxide at high temperature, and then further oxidized to generate nitrogen dioxide, which generates high-temperature low-concentration nitric acid with water generated by incineration. Although the concentration of generated nitric acid is low, its chemical activity is significantly enhanced in a high-temperature environment, and the corrosion of low-concentration high-temperature nitric acid to the incinerator equipment is significantly increased. SUMMARY

[0007] The purpose of the present application is to solve the problems existing in the organic waste liquid treatment technology, and provide a recovery method for recovering deuterium from deuterium-containing organic waste liquid.

[0008] The purpose of the present application is solved by the following technical scheme:

[0009] A recovery method for recovering deuterium from deuterium-containing organic waste liquid, characterized in that the steps of the recovery method are as follows:

[0010] A, after adjusting the incinerator to a negative pressure state, igniting, and after successful ignition, entering step B;

[0011] B, the inert gas as atomization medium, the pure oxygen as combustion-supporting gas, and the deuterium-containing organic waste liquid as incineration material are mixed into atomized gas-liquid by an atomizing burner, and then sprayed into the incinerator;

[0012] C, after the atomized gas-liquid is fully incinerated in the incinerator with a temperature of 1100℃ or above and an inner wall temperature controlled at 200-300℃, the flue gas containing carbon dioxide and deuterium-containing water is discharged from the incinerator and enters a primary heat exchanger;

[0013] D. The primary heat exchanger uses cooling water to cool the flue gas and recover the deuterium-containing water from the flue gas. After the cooled flue gas exits the primary heat exchanger, it enters the secondary heat exchanger.

[0014] E. The secondary heat exchanger uses chilled water to further cool the cooled flue gas and continues to recover deuterium-containing water from the flue gas. After the low-temperature flue gas exits the secondary heat exchanger, it is sent into the exhaust pipe by an induced draft fan.

[0015] The recycling method further includes the following steps:

[0016] F. After the exhaust gas in the exhaust pipe is stably discharged, proceed to step G;

[0017] G. Part of the exhaust gas is discharged directly, and the other part of the exhaust gas is used as recirculated gas and mixed with the inert gas in step B through the exhaust gas recirculation pipe to form a new atomizing medium, which then enters step H.

[0018] Steps H, B, E, and G continue to run.

[0019] The primary heat exchanger in step D can recover 20% to 35% of the deuterium-containing water in the flue gas, and the secondary heat exchanger in step E can recover 65% to 80% of the deuterium-containing water in the flue gas.

[0020] When all the exhaust gas in the exhaust pipe in step E is directly discharged, the deuterium-containing water recovery rate in the flue gas is 90%-95%; when part of the exhaust gas in the exhaust pipe in step E is used as recirculated gas and mixed with the inert gas in step B through the exhaust gas recirculation pipe to form a new atomizing medium to continue participating in combustion, the deuterium-containing water recovery rate in the flue gas reaches more than 99.0%.

[0021] In step G, the circulating gas flow rate accounts for 20% to 80% of the exhaust gas flow rate (or the low-temperature flue gas flow rate discharged from the secondary heat exchanger), and the supply of circulating gas mixed with the inert gas in step B to form a new atomizing medium remains unchanged, thereby dynamically adjusting the supply of inert gas.

[0022] The specific process of the exhaust gas recirculation procedure is as follows: After the incinerator has been running normally for 0.5 to 1 hour, the exhaust gas discharge pipe continuously and stably discharges exhaust gas. The exhaust gas recirculation pipe is then opened, and the recirculated exhaust gas enters the atomizing gas valve group pipeline through the recirculating gas buffer tank, the recirculating gas flow meter, and the gas booster pump, maintaining the atomizing gas channel flow meter at 3m. 3 / h~6m 3 / h, and dynamically adjust the flow rate of inert gas according to the flow rate of the circulating gas meter to control the amount of exhaust gas circulation. The proportion of exhaust gas circulation to exhaust gas in the incineration system is 20% to 80%.

[0023] The incinerator ignition process in step A is as follows:

[0024] A1, open the ventilation port of the incinerator, enter step A2;

[0025] A2, adjust the inner cavity of the incinerator to a negative pressure state, ignite the igniter, and then enter step A3;

[0026] A3, after the flame detector detects the flame for 2-3 seconds, the atomizing burner provides atomized gas-liquid to the incinerator, and enters step A4;

[0027] A4, after the atomizing burner provides atomized gas-liquid to the incinerator for no less than 10 seconds, the igniter is automatically extinguished, if the flame detector detects the flame, it enters step A5, if the flame detector does not detect the flame, it enters step A6;

[0028] A5, close the ventilation port and continue to provide atomized gas-liquid to the incinerator by the atomizing burner, and enter step B stably;

[0029] A6, start the induced draft fan to replace the combustible gas in the incinerator based on the air entering through the ventilation port, and enter step A7 after a period of time (generally more than 30 minutes);

[0030] A7, the combustible gas detection device detects the combustible gas content of the incinerator, and returns to step A2 if the detection is qualified, or continues to replace the combustible gas in the incinerator if the detection is unqualified.

[0031] The combustible gas content detection standard in step A7 is that the concentration of benzene in the phenoxy mixed gas is less than 1200 ppm (0.12 vol%), and the reading is stably controlled below 10% LEL when detecting the combustible gas.

[0032] The negative pressure state of the incinerator in step A is -50 Pa to -100 Pa.

[0033] During the stable operation of the incinerator, the primary heat exchanger, and the secondary heat exchanger, the incinerator, the primary heat exchanger, and the secondary heat exchanger located before the induced draft fan form a connected system, and the pressures at each place are the same, all being -50 Pa to -100 Pa; the tail gas in the tail gas discharge pipe located after the induced draft fan is under positive pressure (30 KPa to 40 KPa).

[0034] The deuterium-containing organic waste liquid in step B is a deuterium-containing organic waste liquid generated by a chemical project, or a mixed liquid of a deuterium-containing organic waste liquid directly generated by a chemical project and a low-carbon alcohol; the volume ratio of the deuterium-containing organic waste liquid to the low-carbon alcohol in the mixed liquid is 1:0.4-0.6, and the low-carbon alcohol is a C1-C5 straight-chain or branched-chain alcohol.

[0035] Preferably, the low-carbon alcohol is methanol, ethanol, or isopropyl alcohol; further preferably, the low-carbon alcohol is ethanol.

[0036] The deuterium-containing organic waste liquid in step B is fed with pure oxygen in a complete reaction stoichiometric molar ratio, wherein the feeding amount of pure oxygen is 1.2 to 1.8 times of its stoichiometric molar ratio; the feeding ratio of the deuterium-containing organic waste liquid in step B to inert gas is 1:(0.4-0.6) kg·h -1 / m 3 ·h -1 ; the flow rate of the inert gas in step B is 3m 3 / h-6m 3 / h.

[0037] The flue gas temperature output by the incinerator in step C is 500℃-600℃, the temperature of the cooled flue gas output by the primary heat exchanger in step D is 100℃-200℃; the low-temperature flue gas temperature output by the secondary heat exchanger in step F is 2℃-5℃.

[0038] The incinerator in step C and the primary heat exchanger in step D are connected in parallel to the cooling tower, the cooling water temperature supplied by the cooling tower to the incinerator and the primary heat exchanger is 25℃-50℃, the cooling water flow rate supplied by the cooling tower to the incinerator is 3m 3 / h-12m 3 / h, and the temperature rise of the recirculating cooling water is 5℃-23℃; the cooling water flow rate supplied by the cooling tower to the primary heat exchanger is 1m 3 / h-2m 3 / h, and the temperature rise of the recirculating cooling water is 8℃-17℃; the secondary heat exchanger in step F uses chilled brine with a temperature of 0℃-3℃ for cooling, and the chilled brine flow rate supplied to the secondary heat exchanger is 3m 3 / h-4m 3 / h, and the temperature rise of the recirculating chilled brine is 2℃-3℃.

[0039] The recovery system used in the recovery method includes a feeding device, an incineration device including an ignition mechanism, a cooling circulation device, and a draft fan, wherein the feeding device is responsible for spraying atomized gas-liquid into the incineration device, the atomized gas-liquid is formed by mixing inert gas as an atomizing medium, pure oxygen as a combustion-supporting gas, and deuterium-containing organic waste liquid as an incineration material in a certain proportion into an atomizing burner; after the incineration device is ignited, the atomized gas-liquid is fully incinerated to generate flue gas containing carbon dioxide and deuterium-containing water, which is discharged into the cooling circulation device; the cooling circulation device cools the flue gas by a stepwise cooling method and recovers the deuterium-containing water in the flue gas, the remaining low-temperature flue gas after the deuterium-containing water is recovered is discharged through a tail gas discharge pipe, or part of it is discharged and the other part returns to the feeding device to continue participating in incineration; the draft fan is used to maintain a negative pressure state in the incinerator of the incineration device, to provide circulating air when the incineration device is ignited, and to guide and accelerate the circulation of flue gas generated by incinerating atomized gas-liquid in the incinerator.

[0040] The recovery system further comprises a tail gas recycling device, which can deliver 20-80% of the tail gas to the feeding device to continue the incineration.

[0041] The tail gas recycling device comprises a tail gas recycling pipe, a recycling gas buffer tank, a recycling gas flow meter and a gas booster pump. One end of the tail gas recycling pipe is connected to the tail gas discharge pipe through a three-way valve, and the other end is connected to the atomizing gas valve group pipe. The recycling gas buffer tank, the recycling gas flow meter and the gas booster pump are arranged in sequence on the tail gas recycling pipe in the direction from the tail gas discharge pipe to the atomizing gas valve group pipe. The recycling gas flow meter and the gas booster pump are interlocked.

[0042] The pressure range of the gas booster pump is 30-40 KPa at the inlet side and 0.3-0.4 MPa at the outlet side.

[0043] The feeding device comprises a deuterium-containing organic waste liquid storage tank, a diaphragm pump (pressurized to 0.3-0.4 MPa), a waste liquid valve group pipe, an atomizing gas valve group pipe, an oxygen valve group pipe and an atomizing burner. The deuterium-containing organic waste liquid storage tank is connected to the front end of the waste liquid valve group pipe through the diaphragm pump. A pressure stabilizing valve, a flow meter and an adjusting valve are arranged in sequence on the waste liquid valve group pipe. The tail end of the waste liquid valve group pipe is connected to the incineration material inlet of the atomizing burner. One end of the atomizing gas valve group pipe is connected to an inert gas supply device, and the other end is connected to the atomizing medium inlet of the atomizing burner. A pressure stabilizing valve and a flow meter are arranged in sequence on the atomizing gas valve group pipe. The tail gas recycling pipe is connected to the atomizing gas valve group pipe before the pressure stabilizing valve. One end of the oxygen valve group pipe is connected to a pure oxygen supply device, and the other end is connected to the combustion-supporting gas inlet of the atomizing burner. A pressure stabilizing valve, a flow meter and an adjusting valve are arranged in sequence on the oxygen valve group pipe. The atomizing burner is installed at the front end inlet of the incinerator in the incineration device.

[0044] A check valve for preventing liquid backflow and a damper for reducing flow pulsation are arranged between the diaphragm pump and the front end of the waste liquid valve group pipe.

[0045] The incineration device comprises an incinerator, at least one igniter arranged on the periphery of the front end inlet of the incinerator, the igniter being connected with a natural gas storage tank through a pipeline and the igniter and the natural gas storage tank forming an ignition mechanism; the incinerator has a refractory layer, a steel inner cylinder and a steel cooling jacket from inside to outside of the incineration chamber, a flame detector for detecting the ignition effect of the igniter is arranged on the front side of the inner cavity of the incineration chamber, a pressure detection device for monitoring the pressure state inside the incineration chamber is arranged on the incinerator, and a plurality of temperature detection devices are uniformly arranged in the incineration chamber, the cooling jacket is connected with a cooling tower through a cooling circulation pipeline with a cooling circulation water pump, and at least one temperature detection device is arranged on the cooling jacket, and temperature detection devices or temperature detection devices and pressure detection devices are arranged on the cooling circulation pipeline at the inlet and outlet of the cooling jacket respectively; a ventilation opening communicating with the incineration chamber is arranged on the incinerator, the tail end of the incinerator is connected with a primary heat exchanger through a flue gas output pipe, and the flue gas output pipe is provided with a bursting disc and a temperature detection device.

[0046] The purpose of arranging the bursting disc is to prevent the pressure in the furnace from rising sharply due to abnormal conditions during the operation of the incinerator, and the bursting disc can quickly break when the pressure reaches the set burst pressure, thereby releasing the high-pressure gas in the furnace and preventing the furnace body from exploding due to overpressure.

[0047] The bottom of the incinerator is provided with a drain pipe with a valve.

[0048] The cooling circulation device comprises a primary heat exchanger and a secondary heat exchanger, the inlet of the primary heat exchanger is connected with the outlet of the incinerator in the incineration device through a flue gas output pipe, the outlet of the primary heat exchanger is connected with the inlet of the secondary heat exchanger through a cooling flue gas output pipe, the outlet of the secondary heat exchanger is connected with an induced draft fan through a low-temperature flue gas output pipe, a primary condensate pipe is arranged at the bottom of the primary heat exchanger, and a secondary condensate pipe is arranged at the bottom of the secondary heat exchanger; the refrigerant inlet and outlet of the primary heat exchanger are connected with a cooling tower through a cooling circulation pipeline with a cooling circulation water pump, and temperature detection devices or temperature detection devices and pressure detection devices are arranged on the cooling circulation pipeline at the inlet and outlet of the primary heat exchanger respectively; the refrigerant inlet and outlet of the secondary heat exchanger are connected with a refrigerated brine unit through a refrigeration circulation pipeline with a refrigeration circulation water pump, and temperature detection devices or temperature detection devices and pressure detection devices are arranged on the refrigeration circulation pipeline at the inlet and outlet of the secondary heat exchanger respectively.

[0049] The cooling jacket on the incinerator and the primary heat exchanger are connected in parallel and then connected in series with the cooling tower.

[0050] Compared with the prior art, the present application has the following advantages:

[0051] The recycling method can fully incinerate the deuterium-containing organic waste liquid, and no waste residue and harmful gas are discharged, and when part of the tail gas participates in the circulation, the high-value deuterium recovery rate can reach 99.0% or more.

[0052] The recycling method provided by the application uses pure oxygen as combustion-supporting gas, which can ensure that the deuterium-containing organic waste liquid is fully incinerated to improve the deuterium recovery rate, and prevent the high-temperature nitrogen oxide acidic gas generated by air combustion from reacting with water to cause corrosion to the equipment.

[0053] The incinerator provided by the application adopts a semi-closed system to prevent air circulation from taking away the deuterium-containing water and avoid loss of high-value heavy water, so that the deuterium recovery rate can reach 99.0% or more.

[0054] The recycling method provided by the application uses inert gas argon as atomizing gas in the early stage, and uses part of the tail gas as circulating gas and inert gas to form atomizing gas in the middle and late stages, which can not only improve the safety factor of the incinerator, but also reduce the temperature of the incinerator hearth by using the condensed tail gas circulating gas, and further reduce the loss of deuterium-containing water and improve the deuterium recovery rate.

[0055] The furnace body of the incinerator is provided with a steel cooling jacket to realize heat exchange, actively cool the furnace body, control the inner wall temperature of the furnace to be kept at 200-300 DEG C, and realize continuous and stable incineration of the system.

[0056] The explosion disc, the front, middle and rear temperature detection devices and the pressure detection device arranged in the recycling system improve the safety performance of the whole device and the state analysis of the system operation. BRIEF DESCRIPTION OF DRAWINGS

[0057] ATTACH Figure 1 The recycling method for recovering deuterium from deuterium-containing organic waste liquid provided by the application adopts the recycling system flow chart;

[0058] ATTACH Figure 2 The ignition method flow chart in the recycling method for recovering deuterium from deuterium-containing organic waste liquid provided by the application.

[0059] Wherein: 1—Deuterium-containing organic waste liquid storage tank; 2—Diaphragm pump; 3—Waste liquid valve group pipeline; 4—Atomizing gas valve group pipeline; 5—Oxygen valve group pipeline; 6—Atomizing burner; 7—Natural gas storage tank; 8—Igniter; 9—Incinerator; 10—Ventilation opening; 11—Flame detector; 12—Cooling jacket; 13—Flue gas output pipe; 14—Rupture disc; 15—Cooling tower; 16—Cooling circulating water pump; 17—Cooling circulating pipeline; 1 8—First-stage heat exchanger; 19—First-stage condensate pipe; 20—Cooling flue gas outlet pipe; 21—Refrigerated brine unit; 22—Refrigerated circulating water pump; 23—Refrigerated circulating pipeline; 24—Second-stage heat exchanger; 25—Second-stage condensate pipe; 26—Low-temperature flue gas outlet pipe; 27—Exhaust fan; 28—Tail gas discharge pipe; 29—Tail gas circulation pipe; 30—Circulating gas buffer tank; 31—Circulating gas flow meter; 32—Gas booster pump. Detailed Implementation

[0060] Exemplary embodiments will now be described more fully with reference to the accompanying drawings. However, these exemplary embodiments can be implemented in many forms and should not be construed as limited to the embodiments set forth herein; rather, they are provided so that the invention will be thorough and complete, and the concept of the exemplary embodiments will be fully conveyed to those skilled in the art. The same reference numerals in the drawings denote the same or similar structures, and therefore their detailed description will be omitted.

[0061] The terms “a,” “one,” “the,” and “the” are used to indicate the existence of one or more elements / components / etc.; the terms “including” and “having” are used to indicate an open-ended meaning of inclusion and that other elements / components / etc. may exist in addition to the listed elements / components / etc.

[0062] like Figures 1-2 The following is a method for recovering deuterium from deuterium-containing organic waste liquid:

[0063] A. After adjusting the incinerator 9 to a negative pressure state of -50Pa to -100Pa, ignite it. After successful ignition, proceed to step B.

[0064] The ignition process of incinerator 9 in step A is as follows:

[0065] A1. Open the ventilation opening 10 of the incinerator 9 and proceed to step A2;

[0066] A2. Adjust the inner cavity of the incinerator 9 to a negative pressure state, and after the igniter 8 is ignited, proceed to step A3.

[0067] A3. After the flame detector 11 detects the flame for 2 to 3 seconds, the atomizing burner 6 supplies the proportionally configured atomized gas and liquid to the incinerator 9 and proceeds to step A4.

[0068] A4, after the atomizing burner 6 provides atomizing gas-liquid to the incinerator 9 for no less than 10 seconds, the igniter 8 is automatically extinguished, if the flame detector 11 detects flame, the ignition is successful and enters step A5, if the flame detector 11 does not detect flame, the ignition is unsuccessful and enters step A6;

[0069] A5, the air vent 10 is closed and the atomizing burner 6 continues to provide atomizing gas-liquid to the incinerator 9, and enters step B stably;

[0070] A6, the induced draft fan 27 is started to replace the combustible gas in the incinerator 9 based on the air entering the air vent 10, and enters step A7 after a period of time;

[0071] A7, the combustible gas detection device detects the combustible gas content of the incinerator 9, and returns to step A2 after the detection is qualified, and returns to step A6 to continue to replace the combustible gas in the incinerator 9 after the detection is unqualified;

[0072] B, the inert gas as the atomizing medium, the pure oxygen as the combustion-supporting gas, and the deuterium-containing organic waste liquid as the incineration object are mixed by the atomizing burner 6 into atomizing gas-liquid and sprayed into the incinerator 9, wherein the deuterium-containing organic waste liquid and the pure oxygen are fed according to the stoichiometric molar ratio of complete reaction (the feeding amount of the pure oxygen is 1.2 to 1.8 times of the stoichiometric molar ratio), the feeding ratio of the deuterium-containing organic waste liquid to the inert gas is 1:(0.4-0.6) kg·h -1 / m 3 ·h -1 , and the flow rate of the inert gas is 3m 3 / h-6m 3 / h;

[0073] C, after the atomizing gas-liquid is fully incinerated in the incinerator 9 with a temperature above 1100℃ and an inner wall temperature controlled at 200℃-300℃, the flue gas containing carbon dioxide and deuterium-containing water is discharged from the incinerator 9 and enters the primary heat exchanger 18, and the flue gas temperature output from the incinerator 9 is 500℃-600℃;

[0074] D, the primary heat exchanger 18 uses cooling water to cool the flue gas and recover the deuterium-containing water in the flue gas, and the cooled flue gas with a temperature of 100℃-200℃ is discharged from the primary heat exchanger 18 and enters the secondary heat exchanger 24;

[0075] E, the secondary heat exchanger 24 uses chilled water to cool the cooled flue gas again and continue to recover the deuterium-containing water in the flue gas, and the low-temperature flue gas with a temperature of 2℃-5℃ is discharged from the secondary heat exchanger 24 and sent to the tail gas discharge pipe 28 by the induced draft fan 27;

[0076] F, after the tail gas in the tail gas discharge pipe 28 is stably discharged, it enters step G;

[0077] G. Part of the exhaust gas is discharged directly, and another part of the exhaust gas is used as recirculated gas and mixed with the inert gas in step B through the exhaust gas recirculation pipe 29 to form a new atomizing medium. The recirculated gas accounts for 20% to 80% of the low-temperature flue gas discharged from the secondary heat exchanger 24, and the supply of the recirculated gas mixed with the inert gas in step B to form a new atomizing medium remains unchanged, thereby dynamically adjusting the supply of inert gas and proceeding to step H.

[0078] Steps H, B, E, and G continue to run.

[0079] Overall, the primary heat exchanger 18 in step D can recover 20%–35% of the deuterium-containing water in the flue gas, and the secondary heat exchanger 24 in step E can recover 65%–80% of the deuterium-containing water in the flue gas. Specifically, when all the exhaust gas in the exhaust pipe 28 in step E is directly discharged, the deuterium-containing water recovery rate in the flue gas is 90%–95%; when part of the exhaust gas in the exhaust pipe 28 in step E is used as recirculated gas and mixed with the inert gas in step B through the exhaust gas recirculation pipe 29 to form a new atomizing medium to continue participating in combustion, the deuterium-containing water recovery rate in the flue gas reaches over 99.0%.

[0080] In step B, the deuterium-containing organic waste liquid is generated from a chemical project. However, to optimize the deuterium-containing organic waste liquid, step B is a mixture of the deuterium-containing organic waste liquid from the chemical project and a low-carbon alcohol. The purpose of preparing the low-carbon alcohol is threefold: First, the low-carbon alcohol has a high oxygen content, providing active oxygen free radicals, which can accelerate the breaking of the molecular chain of the waste liquid and reduce the ignition temperature; the low-carbon alcohol has a low latent heat of vaporization, which can promote the atomization of the waste liquid, improve the gas-solid mixing efficiency, and enhance the incineration efficiency; second, the low-carbon alcohol has a high H / C ratio, which can compensate for the hydrogen deficiency of the high-carbon waste liquid and inhibit the coke formation rate; third, the low-carbon alcohol contains only C / H / O elements, avoiding the introduction of heteroatoms and eliminating acidic gases and dioxin synthesis precursors from the source. The aforementioned low-carbon alcohol is a C1-C5 straight-chain or branched-chain alcohol. Preferably, the low-carbon alcohol is methanol, ethanol, or isopropanol. More preferably, the low-carbon alcohol is ethanol. The volume ratio of the deuterium-containing organic waste liquid to the low-carbon alcohol in the mixture is 1:0.4-0.6.

[0081] In the above recycling method, the incinerator 9 in step C and the primary heat exchanger 18 in step D are connected in parallel and then connected to the cooling tower 15. The cooling water supplied by the cooling tower 15 to the incinerator 9 and the primary heat exchanger 18 has a temperature of 25℃~50℃, and the cooling water flow rate supplied by the cooling tower 15 to the incinerator 9 is 3m³. 3 / h~12m 3 / h, the temperature rise of the return cooling water is 5℃~23℃; the cooling water flow rate supplied by cooling tower 15 to primary heat exchanger 18 is 1m³ / h. 3 / h~2m 3 / h, the temperature rise of the backflow cooling water is 8-17°C; the secondary heat exchanger 24 in step F is cooled by refrigerated brine with a temperature of 0-3°C, and the flow rate of the refrigerated brine supplied to the secondary heat exchanger 24 is 3-4 m 3 / h~4m 3 / h, the temperature rise of the backflow refrigerated brine is 2-3°C.

[0082] As shown in Figure 1 the recycling system used in the recycling method includes a feeding device, a burning device including an ignition mechanism, a cooling circulation device, a tail gas circulation device, and an induced draft fan 27, wherein the feeding device is responsible for spraying the atomized gas-liquid into the burning device, the atomized gas-liquid is formed by mixing inert gas as atomizing medium, pure oxygen as combustion-supporting gas, and deuterium-containing organic waste liquid as burning material in a certain proportion into an atomizing burner 6; the atomized gas-liquid is fully burned in the burning device after ignition to generate flue gas containing carbon dioxide and deuterium-containing water, which is discharged into the cooling circulation device; the cooling circulation device cools the flue gas by stepwise cooling and recovers the deuterium-containing water in the flue gas, and the remaining low-temperature flue gas is discharged through a tail gas discharge pipe 28, or part of it is discharged and the other part returns to the feeding device to continue to participate in the burning; the tail gas circulation device can deliver 20%-80% of the tail gas to the feeding device to continue to participate in the burning; the induced draft fan 27 is used to maintain a negative pressure state in the burning furnace 9 of the burning device, to provide circulating air when the burning device is ignited, and to guide and accelerate the circulation of the flue gas generated by burning the atomized gas-liquid in the burning furnace 9.

[0083] Specifically, the feeding device includes a deuterium-containing organic waste liquid storage tank 1, a diaphragm pump 2, a waste liquid valve group pipeline 3, an atomized gas valve group pipeline 4, an oxygen valve group pipeline 5, and an atomizing burner 6, the deuterium-containing organic waste liquid storage tank 1 is connected to the front end of the waste liquid valve group pipeline 3 through the diaphragm pump 2, a pressure stabilizing valve, a flow meter, and a regulating valve are arranged in sequence on the waste liquid valve group pipeline 3, and the tail end of the waste liquid valve group pipeline 3 is connected to the burning material inlet of the atomizing burner 6; one end of the atomized gas valve group pipeline 4 is connected to an inert gas supply device, the other end is connected to the atomizing medium inlet of the atomizing burner 6, a pressure stabilizing valve and a flow meter are arranged in sequence on the atomized gas valve group pipeline 4, and a tail gas circulation pipe 29 is connected to the front side of the pressure stabilizing valve; one end of the oxygen valve group pipeline 5 is connected to a pure oxygen supply device, the other end is connected to the combustion-supporting gas inlet of the atomizing burner 6, a pressure stabilizing valve, a flow meter, and a regulating valve are arranged in sequence on the oxygen valve group pipeline 5; the atomizing burner 6 is installed at the front end inlet of the burning furnace 9 in the burning device.

[0084] In use, the deuterium-containing organic waste liquid in the deuterium-containing organic waste liquid storage tank 1 enters the inlet of the waste liquid valve group pipeline 3 through the diaphragm pump 2, enters the atomizing burner 6 through the pressure stabilizing valve, flow meter and regulating valve, the inert gas is argon, the argon enters the atomizing burner 6 through the pressure stabilizing valve and flow meter on the inert gas valve group pipeline 4, the oxygen enters the atomizing burner 6 through the pressure stabilizing valve, flow meter and regulating valve on the oxygen valve group pipeline 5, and the three components are mixed according to the set proportion and sprayed out through the atomizing burner 6.

[0085] Specifically, the incineration device comprises a natural gas storage tank 7, an igniter 8, an incineration furnace 9, a ventilation port 10, a flame detector 11, a cooling jacket 12, a flue gas output pipe 13, a bursting disc 14, a temperature detection device and a pressure detection device, at least one igniter 8 is arranged on the front end inlet side of the incineration furnace 9, the igniter 8 is connected with the natural gas storage tank 7 through a pipeline and the igniter 8 and the natural gas storage tank 7 constitute an ignition mechanism, the incineration furnace 9 has a refractory layer, a steel inner cylinder and a steel cooling jacket 12 from inside to outside of the incineration chamber, the flame detector 11 for detecting the ignition effect of the igniter 8 is arranged on the front side of the inner cavity of the incineration chamber, the pressure detection device for monitoring the pressure state in the incineration chamber is arranged on the incineration furnace 9 and a plurality of temperature detection devices are uniformly distributed in the incineration chamber (three temperature detection devices are arranged at front, middle and rear positions according to the flue gas flow direction), the cooling jacket 12 is connected with the cooling tower 15 through the cooling circulation pipeline 17 with a cooling circulation pump 16 and at least one temperature detection device is arranged on the cooling jacket 12, the temperature detection device or the temperature detection device and the pressure detection device are arranged on the cooling circulation pipeline 17 at the inlet and outlet sides of the cooling jacket 12, the ventilation port 10 communicating with the incineration chamber is arranged on the incineration furnace 9, the tail end of the incineration furnace 9 is connected with the primary heat exchanger 18 through the flue gas output pipe 13, and the flue gas output pipe 13 is provided with the bursting disc 14 and the temperature detection device, and the net discharge pipe with a valve is arranged at the bottom of the incineration furnace 9.

[0086] Specifically, the cooling circulation device comprises a first heat exchanger 18 and a second heat exchanger 24, the inlet of the first heat exchanger 18 is connected to the outlet of the incinerator 9 in the incineration device through the flue gas output pipe 13, the outlet of the first heat exchanger 18 is connected to the inlet of the second heat exchanger 24 through the cooling flue gas output pipe 20, the outlet of the second heat exchanger 24 is connected to the induced draft fan 27 through the low-temperature flue gas output pipe 26, the bottom of the first heat exchanger 18 is provided with a first condensate pipe 19, and the bottom of the second heat exchanger 24 is provided with a second condensate pipe 25; the refrigerant inlet and outlet of the first heat exchanger 18 are connected in series with the cooling tower 15 through the cooling circulation pipe 17 with the cooling circulation pump 16, and the cooling circulation pipe 17 on the side of the refrigerant inlet and outlet of the first heat exchanger 18 is respectively provided with a temperature detection device or a temperature detection device and a pressure detection device; the refrigerant inlet and outlet of the second heat exchanger 24 are connected in series with the refrigerated brine unit 21 through the refrigeration circulation pipe 23 with the refrigeration circulation pump 22, and the refrigeration circulation pipe 23 on the side of the refrigerant inlet and outlet of the second heat exchanger 24 is respectively provided with a temperature detection device or a temperature detection device and a pressure detection device.

[0087] Specifically, the tail gas circulation device comprises a tail gas circulation pipe 29, a circulating gas buffer tank 30, a circulating gas flow meter 31 and a gas booster pump 32, one end of the tail gas circulation pipe 29 is connected to the tail gas discharge pipe 28 through a three-way valve, and the other end is connected to the atomizing gas valve group pipe 4, the circulating gas buffer tank 30, the circulating gas flow meter 31 and the gas booster pump 32 are arranged in sequence on the tail gas circulation pipe 29 from the tail gas discharge pipe 28 to the atomizing gas valve group pipe 4, and the circulating gas flow meter 31 and the gas booster pump 32 are interlocked.

[0088] In the recycling system provided by the application, the flue gas outlet of the incinerator 9 is connected to the two-stage heat exchanger, the steel cooling jacket 12 of the incinerator 9 and the refrigerant inlet and outlet of the first heat exchanger 18 are connected to the cold water tower in parallel, the refrigerant inlet and outlet of the second heat exchanger 24 are connected to the refrigerated brine unit 21, the bottoms of the first heat exchanger 18 and the second heat exchanger 24 are provided with condensate pipes to connect a condensate storage tank, and the flue gas outlet on the side of the second heat exchanger 24 is provided with an induced draft fan 27. The refrigerant outlets of the cold water tower and the refrigerated brine unit 21 are respectively provided with centrifugal pumps as circulating pumps. Temperature detection devices are arranged at the flue gas and refrigerant outlet ends of the incinerator 9, the first heat exchanger 18 and the second heat exchanger 24. In addition, pressure detection devices are arranged in the incineration chamber, the steel cooling jacket 12 and after the refrigerant delivery pump.

[0089] The tail gas circulation pipe 29 is arranged at the end of the tail gas discharge pipe 28 to circulate a certain amount of tail gas, which enters the front end of the atomizing gas valve group pipe 4 through the circulating gas buffer tank 30, the circulating gas flow meter 31 and the gas booster pump 32, the argon flow is controlled according to the circulating gas flow, and the deuterium-containing organic waste liquid is atomized by using the tail gas circulating gas.

[0090] Embodiment

[0091] The present application provides a recovery system for recovering deuterium from deuterium-containing organic waste liquid, which comprises a feeding device, a burning device comprising an ignition mechanism, a cooling circulation device, a tail gas circulation device, and an air induction fan 27 and a tail gas discharge pipe 28, wherein the feeding device comprises a deuterium-containing organic waste liquid storage tank 1, a diaphragm pump 2, a waste liquid valve group pipe 3, an atomizing gas valve group pipe 4, an oxygen valve group pipe 5, an atomizing burner 6, a pressure stabilizing valve, a flow meter and a regulating valve, and temperature and pressure detection devices; the burning device comprises a natural gas storage tank 7, an igniter 8, a burning furnace 9, a ventilation opening 10, a flame detector 11, a cooling jacket 12, a flue gas output pipe 13, a bursting disc 14, temperature and pressure detection devices; the cooling circulation device comprises a cooling tower 15, a cooling circulation water pump 16, a cooling circulation pipe 17, a primary heat exchanger 18, a primary condensate water pipe 19, a flue gas output pipe 20, a refrigerated brine unit 21, a refrigerated circulation water pump 22, a refrigerated circulation pipe 23, a secondary heat exchanger 24, a secondary condensate water pipe 25, and a low-temperature flue gas output pipe 26; the tail gas circulation device comprises a tail gas circulation pipe 29, a circulation gas buffer tank 30, a circulation gas flow meter 31, and a gas booster pump 32. In use, the feeding device is responsible for spraying the atomized gas-liquid into the burning device, wherein the atomized gas-liquid is formed by mixing inert gas as an atomizing medium, pure oxygen as a combustion-supporting gas, and deuterium-containing organic waste liquid as a burning substance into the atomizing burner 6 in a proper proportion; after ignition, the atomized gas-liquid is fully burned in the burning device to generate flue gas containing carbon dioxide and deuterium-containing water, which is discharged into the cooling circulation device; the cooling circulation device reduces the temperature of the flue gas by a stepwise cooling method and recovers the deuterium-containing water in the flue gas, and the remaining low-temperature flue gas is discharged through the tail gas discharge pipe 28 or part of it is discharged and the other part returns to the feeding device to continue participating in the burning; the tail gas circulation device can transport 20% to 80% of the tail gas to the feeding device to continue participating in the burning; the air induction fan 27 is used to maintain a negative pressure state in the burning furnace 9 of the burning device, to provide circulating air when the burning device is ignited, and to guide and accelerate the circulation of the flue gas generated by burning the atomized gas-liquid in the burning furnace 9.

[0092] The present application provides a recovery method for recovering deuterium from deuterium-containing organic waste liquid, and the specific operation is as follows:

[0093] The air induction fan 27 is turned on to make the furnace pressure reach-75Pa, and the deuterium-containing phenethyl alcohol is set at a flow rate of 10kg / h (deuterium-containing benzene: ethanol = 1:0.5vol), argon at 5m 3 / h, and pure oxygen at 46.6kg / h (wherein the amount of pure oxygen is 1.7 times the stoichiometric molar amount); when ignited, the three components are sprayed out simultaneously through the atomizing burner 6; after successful ignition, the temperature in the burning area of the burning furnace 9 is gradually increased to 1100℃ within 0.5h, the burning furnace 9 achieves stable operation, the supply temperature of the cooling water is 30℃, and the flow rate of the cooling water in the cooling jacket 12 is 3m3 / h, the temperature rise of the cooling water at the inlet and outlet of the cooling jacket 12 was 23°C, the wall temperature of the incinerator 9 was maintained at 260°C, and the temperature of the flue gas output from the incinerator was 530°C; the flow rate of the cooling water in the primary heat exchanger 18 was 1.7 m 3 / h, the temperature rise of the cooling water was 10°C, and the temperature of the cooled flue gas output from the primary heat exchanger was 130°C; the supply temperature of the chilled brine in the secondary heat exchanger 24 was 0°C, the flow rate of the chilled brine was 3 m 3 / h, the temperature rise of the chilled brine was 3°C, and the temperature of the low-temperature flue gas output from the secondary heat exchanger 24 was 3°C. After the incinerator 9 had been operated for 0.5 h, the tail gas circulation pipe 29 was opened, and the flow rate of the circulating gas was controlled to be 4 m 3 / h, the flow rate of the argon gas was 1 m 3 / h, the CO content of the flue gas detected at the secondary heat exchanger 24 was 0 ppm, and after the incinerator 9 had been operated normally for 5 h, the deuterium-containing water recovery rate data at each stage of the operation of the incinerator were calculated according to the amount of deuterium-containing water collected by the primary condensate pipe 19 and the secondary condensate pipe 25 at each stage of the operation of the incinerator, and the data are shown in Table 1 below:

[0094]

[0095] Table 1 Deuterium-containing water recovery rate data at each stage of the operation of the incinerator

[0096] Comparative Example 1

[0097] The recovery device and the specific operation were the same as in the example, except that the tail gas was not recycled in Comparative Example 1, and thus the deuterium-containing water recovery rate of the primary heat exchanger 18 and the secondary heat exchanger 24 was only 93.7%.

[0098] The reason is that if the tail gas is recycled, the argon gas entering the system at the first stage will be partially recycled, thereby reducing the cost of argon gas; at the same time, the recycled tail gas will carry a certain amount of water vapor, which will re-enter the system for secondary condensation and recovery, thereby reducing the water vapor carried away by the tail gas and improving the deuterium-containing water recovery rate.

[0099] Comparative Example 2

[0100] The recovery device and the specific operation were the same as in the example, except that the tail gas was not recycled in Comparative Example 2, and air was used as the combustion-supporting gas (to ensure that the deuterium-containing organic waste liquid is fully incinerated, the flow rate of air in Comparative Example 2 was 5 times the flow rate of pure oxygen in the example, i.e., the flow rate of air was 233 kg / h), and thus the deuterium-containing water recovery rate of the primary heat exchanger 18 and the secondary heat exchanger 24 was 62.3%, and after the incinerator was operated for 24 h and then stopped, obvious corrosion patterns were detected on the inner wall surface of the incinerator 9.

[0101] The reason is that: in order to ensure that the deuterium-containing waste liquid is fully incinerated, the air flow must be increased, and a large amount of nitrogen gas is introduced, which not only carries away the deuterium-containing water vapor, resulting in a decrease in the recovery rate of the deuterium-containing water, but also causes the nitrogen gas to be oxidized to generate acidic gas under high temperature conditions of incineration, which further generates high-temperature low-concentration nitric acid with the deuterium-containing water, resulting in corrosion of the inner wall of the incinerator 9.

[0102] The recovery method provided by the application can fully incinerate the deuterium-containing organic waste liquid, and no waste residue and harmful gas are discharged, and when no tail gas is involved in the cycle, the high-value deuterium recovery rate can reach 90% to 95%, and when part of the tail gas is involved in the cycle, the high-value deuterium recovery rate can reach more than 99.0%.

[0103] In the embodiments of the present application, the term "a plurality of" refers to two or more, unless otherwise explicitly limited. The terms "mounting", "connecting", "fixing" and the like should be understood in a broad sense, for example, "connecting" can be fixed connection, or detachable connection, or integral connection. For those skilled in the art, the specific meaning of the above terms in the embodiments of the present application can be understood according to the specific circumstances.

[0104] In the description of the embodiments of the present application, it should be understood that the positions or position relationships indicated by the terms "upper", "lower" and the like are based on the positions or position relationships shown in the drawings, and are only for the convenience of describing the embodiments of the present application and simplifying the description, and therefore cannot be understood as indicating or implying that the devices or units referred to must have a specific direction, be constructed and operated in a specific position, and therefore cannot be understood as limiting the embodiments of the present application.

[0105] In the description of the present application, the terms "one embodiment", "one preferred embodiment" and the like mean that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present application. In the present application, the illustrative description of the above terms does not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials or characteristics described can be combined in any one or more embodiments or examples in a suitable manner.

[0106] The above embodiments only illustrate the technical idea of the present application, and cannot limit the protection scope of the present application, and any modification made according to the technical idea of the present application on the basis of the technical scheme falls within the protection scope of the present application; the technologies not involved in the present application can be realized by the prior art.

Claims

1. A method for recovering deuterium from deuterium-containing organic waste liquid, characterized in that: The recycling system used in this recycling method includes a feeding device, an incineration device including an ignition mechanism, a cooling circulation device, and an induced draft fan. The feeding device is responsible for injecting atomized gas and liquid into the incineration device. The atomized gas and liquid is composed of an inert gas as the atomizing medium, pure oxygen as the combustion-supporting gas, and deuterium-containing organic waste liquid as the incinerator, which are mixed by inputting them into the atomizing burner in proportion. After the incineration device is ignited, the atomized gas and liquid are fully burned to generate flue gas containing carbon dioxide and deuterium water, which is discharged into the cooling circulation device. The cooling circulation device cools the flue gas and recovers the deuterium-containing water in the flue gas through a stepped cooling method. After the deuterium-containing water is recovered, the remaining low-temperature flue gas is discharged through the tail gas discharge pipe, or part of it is discharged and the other part is returned to the feeding device to continue to participate in combustion. The induced draft fan is used to keep the incinerator of the incinerator under negative pressure, to provide circulating air when the incinerator is ignited, and to guide the flue gas generated by the combustion atomization gas-liquid in the incinerator. The steps of this recycling method are as follows: A. After adjusting the incinerator to a negative pressure state, ignite it. After successful ignition, proceed to step B. B. The inert gas used as the atomizing medium, the pure oxygen used as the combustion-supporting gas, and the deuterium-containing organic waste liquid used as the incinerator are mixed in proportion through the atomizing burner to form an atomized gas-liquid mixture, which is then injected into the incinerator. C. After the atomized gas and liquid are fully combusted in the incinerator where the temperature in the combustion zone is above 1100℃ and the inner wall temperature is controlled at 200℃~300℃, the generated flue gas containing carbon dioxide and deuterium water is discharged from the incinerator and enters the first-stage heat exchanger. D. The primary heat exchanger uses cooling water to cool the flue gas and recover the deuterium-containing water from the flue gas. After the cooled flue gas exits the primary heat exchanger, it enters the secondary heat exchanger. E. The secondary heat exchanger uses chilled water to further cool the cooled flue gas and continues to recover the deuterium-containing water in the flue gas. After the low-temperature flue gas is discharged from the secondary heat exchanger, it is sent into the exhaust pipe by the induced draft fan. F. After the exhaust gas in the exhaust pipe is stably discharged, proceed to step G; G. Part of the exhaust gas is discharged directly, and the other part of the exhaust gas is used as recirculated gas and mixed with the inert gas in step B through the exhaust gas recirculation pipe to form a new atomizing medium, which then enters step H. Steps H, B, E, and G continue to run.

2. The method for recovering deuterium from deuterium-containing organic waste liquid according to claim 1, characterized in that: In step G, the flow rate of the circulating gas accounts for 20% to 80% of the exhaust gas flow rate, and the supply of the circulating gas mixed with the inert gas in step B to form a new atomizing medium remains unchanged, thereby dynamically adjusting the supply of inert gas.

3. The method for recovering deuterium from deuterium-containing organic waste liquid according to claim 1, characterized in that: The incinerator ignition process in step A is as follows: A1. Open the ventilation opening of the incinerator and proceed to step A2; A2. Adjust the inner cavity of the incinerator to a negative pressure state, and after the igniter is ignited, proceed to step A3. A3. After the flame detector detects the flame for 2 to 3 seconds, the atomizing burner supplies atomized gas and liquid to the incinerator and proceeds to step A4. A4. After the atomizing burner supplies atomized gas and liquid to the incinerator for no less than 10 seconds, the igniter automatically shuts off. If the flame detector detects a flame, the ignition is successful and proceeds to step A5. If the flame detector does not detect a flame, the ignition is unsuccessful and proceeds to step A6. A5. Close the vents while the atomizing burner continues to supply atomized gas and liquid to the incinerator, and proceed to step B in a stable manner; A6. Start the induced draft fan to replace the combustible gas in the incinerator with the air entering through the ventilation opening, and continue for a period of time before proceeding to step A7. A7. The combustible gas detection device detects the combustible gas content in the incinerator. If the test is qualified, return to step A2. If the test is unqualified, return to step A6 to continue replacing the combustible gas in the incinerator.

4. The method for recovering deuterium from deuterium-containing organic waste liquid according to claim 1 or 3, characterized in that: The negative pressure state of the incinerator in step A is -50Pa to -100Pa.

5. The method for recovering deuterium from deuterium-containing organic waste liquid according to claim 1, characterized in that: In step B, the deuterium-containing organic waste liquid is either a deuterium-containing organic waste liquid generated from a chemical project or a mixture of a deuterium-containing organic waste liquid generated from a chemical project and a low-carbon alcohol; the volume ratio of the deuterium-containing organic waste liquid to the low-carbon alcohol in the mixture is 1:0.4 to 0.6, and the low-carbon alcohol is a C1 to C5 straight-chain or branched alcohol.

6. The method for recovering deuterium from deuterium-containing organic waste liquid according to claim 1 or 5, characterized in that: In step B, the deuterium-containing organic waste liquid and pure oxygen are fed at a stoichiometric molar ratio for complete reaction, wherein the amount of pure oxygen fed is 1.2 to 1.8 times its stoichiometric molar ratio; the feed ratio of the deuterium-containing organic waste liquid and inert gas in step B is 1:(0.4~0.6) kg•h. -1 / m 3 •h -1 The flow rate of the inert gas in step B is 3m. 3 / h~6m 3 / h.

7. The method for recovering deuterium from deuterium-containing organic waste liquid according to claim 1, characterized in that: The flue gas temperature output from the incinerator in step C is 500℃~600℃; the cooled flue gas temperature output from the primary heat exchanger in step D is 100℃~200℃; and the low-temperature flue gas temperature output from the secondary heat exchanger in step F is 2℃~5℃.

8. The method for recovering deuterium from deuterium-containing organic waste liquid according to claim 1 or 7, characterized in that: The incinerator in step C and the primary heat exchanger in step D are connected in parallel and then connected to a cooling tower. The cooling water supplied by the cooling tower to the incinerator and the primary heat exchanger has a temperature of 25℃~50℃, and the cooling water flow rate supplied by the cooling tower to the incinerator is 3m³ / h. 3 / h~12m 3 / h, the temperature rise of the return cooling water is 5℃~23℃; the cooling water flow rate supplied by the cooling tower to the first-stage heat exchanger is 1m³ / h. 3 / h~2m 3 The temperature of the reflux cooling water rises to 8℃~17℃ per hour; the secondary heat exchanger in step F uses chilled brine at a temperature of 0℃~3℃ for cooling, and the flow rate of the chilled brine supplied to the secondary heat exchanger is 3m³ / h. 3 / h~4m 3 / h, the temperature rise of the refluxed chilled brine is 2℃~3℃.

9. The method for recovering deuterium from deuterium-containing organic waste liquid according to claim 1, characterized in that: The recovery system also includes an exhaust gas recirculation device, which can transport 20% to 80% of the exhaust gas to the feeding device for further combustion. The exhaust gas recirculation device includes an exhaust gas recirculation pipe, a recirculation gas buffer tank, a recirculation gas flow meter, and a gas booster pump. One end of the exhaust gas recirculation pipe is connected to the exhaust gas discharge pipe through a three-way valve, and the other end is connected to the atomizing gas valve group pipeline. The recirculation gas buffer tank, the recirculation gas flow meter, and the gas booster pump are arranged sequentially on the exhaust gas recirculation pipe from the exhaust gas discharge pipe to the atomizing gas valve group pipeline, and the recirculation gas flow meter and the gas booster pump are interlocked.

10. The method for recovering deuterium from deuterium-containing organic waste liquid according to claim 1 or 9, characterized in that: The feeding device includes a deuterium-containing organic waste liquid storage tank, a diaphragm pump, a waste liquid valve group pipeline, an atomizing gas valve group pipeline, an oxygen valve group pipeline, and an atomizing burner. The deuterium-containing organic waste liquid storage tank is connected to the front end of the waste liquid valve group pipeline via the diaphragm pump. A pressure stabilizing valve, a flow meter, and a regulating valve are sequentially arranged on the waste liquid valve group pipeline. The rear end of the waste liquid valve group pipeline is connected to the incinerator feed port on the atomizing burner. One end of the atomizing gas valve group pipeline is connected to an inert gas supply device, and the other end is connected to the atomizing medium feed port on the atomizing burner. A pressure stabilizing valve and a flow meter are sequentially arranged on the atomizing gas valve group pipeline, and a tail gas circulation pipe is connected to the atomizing gas valve group pipeline before the pressure stabilizing valve. One end of the oxygen valve group pipeline is connected to a pure oxygen supply device, and the other end is connected to the combustion-supporting gas feed port on the atomizing burner. A pressure stabilizing valve, a flow meter, and a regulating valve are sequentially arranged on the oxygen valve group pipeline. The atomizing burner is installed at the front inlet of the incinerator in the incineration device.

11. The method for recovering deuterium from deuterium-containing organic waste liquid according to claim 1 or 9, characterized in that: The incineration device includes an incinerator. At least one igniter is arranged around the inlet of the incinerator. The igniter is connected to a natural gas storage tank via a pipeline, and the igniter and the natural gas storage tank constitute an ignition mechanism. The incinerator has a refractory layer, a steel inner cylinder, and a steel cooling jacket from the inside to the outside of the incineration chamber. A flame detector for verifying the ignition effect of the igniter is arranged on the front side of the inner cavity of the incineration chamber. A pressure detection device for monitoring the internal pressure of the incineration chamber is arranged on the incinerator, and multiple temperature detection devices are evenly distributed in the incineration chamber. The cooling jacket is connected to a cooling tower in series via a cooling circulation pipeline with a cooling circulating water pump, and at least one temperature detection device is arranged on the cooling jacket. Temperature detection devices or a temperature detection device and a pressure detection device are respectively arranged on the cooling circulation pipelines on the inlet and outlet sides of the cooling jacket. A ventilation opening connecting the incineration chamber is arranged on the incinerator. The tail end of the incinerator is connected to a primary heat exchanger via a flue gas outlet pipe, and the flue gas outlet pipe is equipped with a rupture disc and a temperature detection device.

12. The method for recovering deuterium from deuterium-containing organic waste liquid according to claim 1 or 9, characterized in that: The cooling circulation device includes a primary heat exchanger and a secondary heat exchanger. The inlet of the primary heat exchanger is connected to the outlet of the incinerator in the incineration unit via a flue gas outlet pipe. The outlet of the primary heat exchanger is connected to the inlet of the secondary heat exchanger via a cooling flue gas outlet pipe. The outlet of the secondary heat exchanger is connected to an induced draft fan via a low-temperature flue gas outlet pipe. A primary condensate pipe is installed at the bottom of the primary heat exchanger, and a secondary condensate pipe is installed at the bottom of the secondary heat exchanger. The refrigerant inlet and outlet of the primary heat exchanger are connected in series to a cooling tower via a cooling circulation pipeline equipped with a cooling circulating water pump. Temperature detection equipment or a temperature detection equipment and a pressure detection equipment are respectively installed on the cooling circulation pipelines on the refrigerant inlet and outlet sides of the primary heat exchanger. The refrigerant inlet and outlet of the secondary heat exchanger are connected in series to a chilled brine unit via a chilled circulation pipeline equipped with a chilled water pump. Temperature detection equipment or a temperature detection equipment and a pressure detection equipment are respectively installed on the chilled circulation pipelines on the refrigerant inlet and outlet sides of the secondary heat exchanger.

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