CN112121452A - Desalination system and desalination method for ethylene glycol barren solution containing high-solubility salt in deep sea natural gas exploitation - Google Patents

Desalination system and desalination method for ethylene glycol barren solution containing high-solubility salt in deep sea natural gas exploitation Download PDF

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Publication number
CN112121452A
CN112121452A CN202011029882.6A CN202011029882A CN112121452A CN 112121452 A CN112121452 A CN 112121452A CN 202011029882 A CN202011029882 A CN 202011029882A CN 112121452 A CN112121452 A CN 112121452A
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tank
negative pressure
salt
valve
pipeline
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Inventor
唐文献
何佳伟
齐继阳
薛少锋
刘波
王�锋
肖尊坤
李华
张建
陈晨
王文涛
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Jiangsu University of Science and Technology
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Jiangsu University of Science and Technology
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Priority to CN202011029882.6A priority Critical patent/CN112121452A/en
Publication of CN112121452A publication Critical patent/CN112121452A/en
Priority to PCT/CN2021/078290 priority patent/WO2022062315A1/en
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/06—Flash distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/42—Regulation; Control
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00—Halides of sodium, potassium or alkali metals in general
    • C01D3/04—Chlorides
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
    • C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
    • C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination

Abstract

The invention discloses a desalination system of glycol barren solution containing high-solubility salt in deep sea natural gas exploitation, which comprises an MEG barren solution recovery device, a salt-containing glycol barren solution flash evaporation device and a first-order salt recovery device. The system efficiently realizes the desalting recovery and the reutilization of the saline glycol barren solution for the deep sea natural gas exploitation, and greatly reduces the loss of glycol so as to reduce the use cost; the monovalent salt NACL crystal in the saline glycol barren solution is extracted and can be used for subsequent deep processing, thereby improving the economic benefit. The invention also discloses a desalination method of the desalination system.

Description

Desalination system and desalination method for ethylene glycol barren solution containing high-solubility salt in deep sea natural gas exploitation
Technical Field
The invention relates to a desalination system and a desalination method for ethylene glycol barren solution containing high-solubility salt in deep sea natural gas exploitation.
Background
In deepwater natural gas field exploitation, natural gas hydrate can be formed due to changes of underwater temperature and pressure to cause blockage of system equipment and pipelines, ethylene glycol is frequently used as a hydrate inhibitor to prevent the blockage of the pipelines and the equipment due to the characteristics of low volatility and easiness in separation from water, and the cyclic utilization of the ethylene glycol is realized by virtue of an ethylene glycol regeneration and recovery system (MRU) in order to reduce cost.
The glycol solution returning from the pipeline generally contains a certain amount of salts after absorbing part of the produced fluid. The traditional ethylene glycol recovery technology is difficult to remove salts in the ethylene glycol, when the salts are more, the salts are easily deposited on the inner surface of a container in the regeneration process when the ethylene glycol is recovered by regeneration, the scaling phenomenon occurs, the pipeline is blocked, and the whole process cannot work normally.
The produced liquid has high salt content in the deep water gas field development, and the existing means is not enough to remove the salt content; the same problems exist in onshore gas field development, such as high salinity in the produced water of Xinjiang Krameri gas field, and the ethylene glycol regeneration system is not desalted, which causes the fouling and blockage in the reboiler.
Disclosure of Invention
The technical problem to be solved by the invention is as follows: provides a desalination system capable of efficiently removing high-solubility salt ions in ethylene glycol barren solution.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows: a desalination system of glycol barren solution containing high-solubility salt in deep sea natural gas exploitation comprises an MEG barren solution recovery device, a salt-containing glycol barren solution flash evaporation device and a first-order salt recovery device;
the device comprises a salt-containing glycol barren solution flash device, a first transportation pump, a first check valve, a first electric valve and a first flow control valve, wherein the salt-containing glycol barren solution flash device is connected with the first transportation pump through a pipeline, the first transportation pump is connected with a negative pressure flash tank through a pipeline, the pipeline between the first transportation pump and the negative pressure flash tank is sequentially provided with the first check valve, the first electric valve and the first flow control valve, the pipeline between the first transportation pump and the check valve is provided with a first temperature transmitter, the pipeline between the electric valve and the flow control valve is provided with a first flow transmitter and a first flow controller, the negative pressure flash tank is provided with two liquid phase outlets and a gas phase outlet positioned at the top of the tank, the gas phase outlet is communicated with the negative pressure condenser through a pipeline, one of the liquid phase outlets is connected with the salt solution tank through a downcomer, the other of the liquid phase outlets is connected with a circulating heater through a second transportation pump, and the outlet of the The flash tank forms a closed loop;
a first pressure controller, a second pressure transmitter and a first pressure gauge which are used for monitoring and controlling the pressure in the negative pressure flash tank in real time are arranged on the negative pressure flash tank, a thermometer and a temperature check meter are also arranged on the negative pressure flash tank, a fourth pressure transmitter and a fifth one-way valve are arranged on a pipeline between the negative pressure flash tank and the second transport pump, a sixth one-way valve and a seventh one-way valve are arranged on a pipeline between the second transport pump and the circulating heater, and a fifth pressure transmitter and a third thermometer are arranged on a pipeline between the sixth one-way valve and the seventh one-way valve; an outlet of the circulating heater is connected with the negative pressure flash tank through a pipeline provided with an eighth one-way valve, and a second pressure controller, a fourth thermometer, a fourth temperature transmitter and a fifth thermometer which are used for ensuring the temperature of the heated MEG barren solution and reaching a specified value are arranged on the pipeline between the eighth one-way valve and the negative pressure flash tank;
the salt-containing glycol barren solution flash evaporation device comprises a negative pressure condenser communicated with a negative pressure flash evaporation tank through a pipeline provided with a second one-way valve, and a first pressure difference transmitter, a second pressure gauge and a second temperature transmitter are arranged on the pipeline between the negative pressure flash evaporation tank and the negative pressure condenser; the negative pressure condenser is connected with the MEG barren liquor receiving tank through a pipeline provided with a third one-way valve and a second electrically operated valve, a third pressure gauge is arranged between the negative pressure condenser and the third one-way valve on the pipeline, and a first conductivity tester, a third temperature transmitter and a temperature controller are arranged on the pipeline between the second electrically operated valve and the MEG barren liquor receiving tank and used for confirming the content of high-solubility monovalent salt ions in MEG barren liquor obtained after flash evaporation; the MEG lean solution receiving tank is provided with a third pressure transmitter, a second thermometer and a liquid level meter; a gas-phase outlet arranged at the top of the MEG lean solution receiving tank is connected with a vacuum pump through a pipeline provided with a vacuum valve, a liquid-phase outlet at the bottom of the MEG lean solution receiving tank is connected with a third transport pump through a third stop valve, a second bypass valve is connected between an inlet of the third stop valve and an outlet of the third transport pump, and the third transport pump is communicated with a qualified MEG lean solution storage tank through a fourth one-way valve;
the monovalent salt recovery system comprises a water tank, the water tank is communicated with the salt liquid tank through a pipeline provided with a fourth transport pump, and a tenth check valve, a fourth electric valve and a second flow control valve are sequentially arranged on the pipeline between an outlet of the fourth transport pump and the salt liquid tank; a fourth pressure gauge is arranged on a pipeline between the fourth transportation pump and the one-way valve, and a second flow transmitter and a second flow controller for controlling the water inflow according to the concentration of the salt solution in the salt solution tank are arranged on a pipeline between the electric valve and the flow control valve; the negative pressure flash tank is connected with the salt liquid tank through a pipeline which is sequentially provided with a ninth one-way valve and a third electric valve, and a seventh thermometer, a second liquid level transmitter, a second liquid level controller, a fifth pressure gauge and a second conductivity tester which are used for monitoring the concentration of the salt solution in the salt liquid tank in real time and maintaining the liquid level in the salt liquid tank to be stable are arranged on the salt liquid tank;
the salt solution tank is respectively connected with a fifth transport pump through a pipeline provided with a fifth stop valve and a pipeline of a fifth bypass valve which are arranged in parallel, an eleventh one-way valve and a fifth electric valve are connected to the pipeline between the fifth transport pump and the centrifugal machine, a sixth pressure transmitter is arranged on the pipeline between the transport pump and the one-way valve, and a third flow transmitter and a third flow controller are arranged on the pipeline between the fifth electric valve and the centrifugal machine; the centrifugal machine is provided with a gas phase outlet positioned at the top and a solid phase outlet positioned at the bottom, wherein the gas phase outlet positioned at the top is communicated with the outside through a pipeline provided with a thirteenth one-way valve, and the solid phase outlet positioned at the bottom is communicated with the salt tank through a pipeline provided with a fourteenth one-way valve.
Preferably, the output port of the first transport pump is further connected to a pipeline between the brine glycol lean solution tank and the first stop valve through a pipeline provided with a first bypass valve to form a first bypass loop, and a first pressure transmitter is installed on a pipeline between a loop connecting port of the first bypass loop and the first stop valve.
As a preferable scheme, a first liquid level transmitter and a first liquid level controller which control the lowest liquid level to ensure the stable quantity of MEG lean liquid flashed in the tank are arranged at the lower part of the inner side of the tank body of the negative pressure flash tank.
Preferably, a second differential pressure transmitter is connected between the pipeline at the outlet end of the sixth one-way valve and the pipeline at the outlet end of the seventh one-way valve.
Preferably, the fourth transport pump forms a bypass circuit by means of a line provided with a fourth shut-off valve and a fourth bypass valve.
As a preferable scheme, an outlet of the bottom circulation loop is arranged on the centrifuge, and the outlet of the circulation loop is connected with the salt solution tank through a pipeline provided with a twelfth one-way valve and a sixth electric valve.
The beneficial effect of this system is:
the system efficiently realizes the desalination recovery and the reutilization of the saline glycol barren solution for the deep sea natural gas exploitation, and greatly reduces the loss of glycol so as to reduce the use cost; the monovalent salt NACL crystal in the saline glycol barren solution is extracted and can be used for subsequent deep processing, thereby improving the economic benefit.
Because the first flow transmitter and the first flow controller are arranged on the pipeline between the electric valve and the flow control valve, the flow in the transport pipe can be adjusted according to the information of pressure, liquid level, temperature and the like in the negative pressure flash tank; the lower part of the inner side of the tank body of the negative pressure flash tank is provided with a first liquid level transmitter and a first liquid level controller which are used for controlling the lowest liquid level so as to ensure the stability of the MEG lean liquor amount flashed in the tank; due to the fact that the second pressure controller, the fourth temperature gauge, the fourth temperature transmitter and the fifth temperature gauge are arranged on the pipeline between the eighth check valve and the negative pressure flash tank, the temperature of the heated MEG lean solution can be guaranteed to reach a specified value. Because be equipped with third pressure transmitter, second thermometer and liquid level appearance on the MEG barren liquor receiving tank, can monitor pressure, temperature and the liquid level in the jar. The salt solution tank is provided with the seventh thermometer, the second liquid level transmitter, the second liquid level controller, the fifth pressure gauge and the second conductivity meter, so that the concentration of the salt solution in the salt solution tank can be monitored in real time, and the liquid level in the salt solution tank can be maintained stable.
The feed liquid transportation in this system has all adopted the mode of bypass return circuit, can guarantee the stability of pipeline in the transportation solution process, improves entire system's security.
The invention aims to solve another technical problem that: provides a desalination method of the desalination system of the glycol barren solution containing high-solubility salt in the deep sea natural gas exploitation.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows: the desalting method of the desalting system for the deep sea natural gas exploitation glycol barren solution containing high-solubility salt comprises the following specific processes:
step 1, flashing saline glycol barren solution:
step 1-1, raw material transportation: in the initial state, valves in each system are in a closed state; the method comprises the steps that firstly, a first stop valve and a first bypass valve are opened, a first transport pump is started, when a bypass loop between a saline ethylene glycol lean solution tank and the first transport pump is filled with MEG lean solution, a first pressure transmitter detects that the pressure in the pipe is stable, then an electric valve is opened through remote control, a first flow control valve is opened, meanwhile, the first bypass valve is closed, and the saline ethylene glycol lean solution raw material is conveyed into a negative pressure flash tank;
step 1-2, flow control: when a first liquid level transmitter on the negative pressure flash tank detects that the solution in the tank reaches a specified liquid level, a first flow control valve on a feeding pipe is controlled through a control system, the flow in the tank is adjusted, and the liquid level of the negative pressure flash tank is maintained to be stable; if an emergency situation occurs suddenly, the first electric valve is directly and remotely closed to prevent the raw materials from flowing in;
step 1-3, cyclic heating: the saline ethylene glycol barren solution flowing into the negative pressure flash tank is transferred to a circulating heater through a second transport pump to be heated and flows back to the negative pressure flash tank again, and a temperature calibrator and a fourth temperature transmitter on the negative pressure flash tank monitor the temperature in the tank in real time to ensure that the temperature in the tank is stabilized at 140 +/-5 ℃;
step 1-4, flash evaporation: the first pressure controller and the second pressure transmitter on the negative pressure flash tank ensure that the operating pressure of the negative pressure flash tank is kept at 15 +/-5 KPa; due to the reduction of the pressure, the ethylene glycol in the negative pressure flash tank starts to carry out flash separation, the temperature supplement is carried out through the circulating heating loop to maintain the temperature required in the flash process, and MEG barren solution is distilled out and accumulated at the top of the negative pressure flash tank in a gas phase form;
step 2, MEG barren solution recovery:
step 2-1, condensing MEG barren solution: the MEG barren liquor gas generated by flash evaporation enters a negative pressure condenser through a second one-way valve, so that the temperature of hot steam is rapidly reduced to 40 +/-3 ℃ to reliquefy the MEG barren liquor gas, then a second electric valve is opened, and the condensate is converged into an MEG barren liquor receiving tank;
step 2-2, purification: opening a vacuum valve and a pneumatic vacuum pump, discharging a small amount of gas in the MEG lean liquid receiving tank, and storing the residual MEG lean liquid into a qualified MEG lean liquid storage tank through a third transport pump;
step 3, monovalent salt recovery:
step 3-1, salt solution storage: the salt solution at the bottom of the negative pressure flash tank obtained in the step 1-4 is conveyed into a salt solution tank through a downcomer, monovalent salt in the salt solution tank reaches a saturated state, crystallization and separation are started, and after the salt concentration in the salt solution tank reaches a set value measured by a second conductivity measuring instrument, the salt solution is conveyed into a centrifuge through a fifth conveying pump for centrifugation;
step 3-2, centrifugal separation: the brine sent to the centrifuge is mixed with some insoluble gas and discharged through a thirteenth one-way valve above the centrifuge, after the residual solid-liquid mixture is centrifuged, the solid salt blocks are stored in a salt tank to be used as the raw material for subsequent deep processing, and the residual solution which is not completely centrifuged flows back into the brine tank through a liquid phase outlet of the centrifuge again;
step 3-3, water injection: when the second liquid level transmitter detects that the liquid level in the brine tank drops to a lower limit value, the second liquid level controller sends a signal, the control system starts the fourth electric valve, water is extracted from the water tank and injected into the brine tank, and the stability of the liquid level in the brine tank is ensured; and when the second conductivity tester detects that the salt concentration in the salt solution tank is lower than a set value, stopping the operation of the centrifuge, closing the fifth electric valve and the fifth transport pump until the next centrifugal treatment condition is met, and turning to the step 3-1 for circulation.
As a preferred scheme, the liquid level in the negative pressure flash tank has set up too high warning of liquid level limit, too high warning of liquid level, too low warning of liquid level and the warning of liquid level limit is crossed to the liquid level excessively through liquid level transmitter, when the liquid level is not in normal range, when having leaded to triggering above warning, handles according to following mode:
when the liquid level of the salt-containing glycol barren solution in the negative pressure flash tank is too high and a liquid level limit too high alarm is triggered, a first electric valve in the feeding loop is cut off to prevent the salt-containing glycol barren solution from immersing a demister or entering a condenser; then, with the continuation of the distillation process, when the liquid level in the negative pressure flash tank is reduced to trigger the alarm of too low liquid level, the feeding loop is opened again;
when the liquid level in the negative pressure flash tank is too low and the liquid level limit is too low to alarm, the circulating heater is closed emergently to control the temperature of the saline glycol barren solution in the negative pressure flash tank to be below 170 ℃; after that, the salt-containing glycol barren solution newly injected into the negative pressure flash tank is slowly distilled due to insufficient heating, the liquid level in the negative pressure flash tank is gradually increased, and when the liquid level is too high, the alarm is triggered, the circulating heater is restarted;
when the liquid level in the negative pressure flash tank is too high, triggering a liquid level overhigh alarm, checking whether a circulating heater is started and the heating value of the circulating heater is the working temperature upper limit value, and if the circulating heater is not started or the heating value of the circulating heater does not reach the working temperature upper limit value, enabling the circulating heater to work according to the heating value as the working temperature upper limit value so as to accelerate the distillation speed of the saline ethylene glycol barren solution in the negative pressure flash tank; if the circulating heater is started at the moment and the heating capacity of the circulating heater reaches the working temperature upper limit value at the moment, reducing the opening degree of a first flow control valve in the feeding loop to reduce the feeding speed;
triggering a liquid level over-low alarm when the liquid level in the negative pressure flash tank is over-low, and adjusting the opening of a first flow control valve in a feeding loop to be maximum; if the feeding flow is maximum, the working temperature of the circulating heater is reduced to the set working temperature value, so that the distillation speed is reduced.
As a preferable scheme, a pressure transmitter at the upper part of the negative pressure flash tank is provided with an over-pressure alarm, a low-pressure alarm and a high-pressure limit alarm, and when the pressure in the negative pressure flash tank is not within a normal range, the corresponding alarm is triggered, the following processing is carried out:
when the pressure in the working temperature upper limit value of the negative pressure flash tank is too low and the pressure too low alarm is triggered, increasing the working temperature of the circulating heater to the working temperature upper limit value;
when the pressure in the negative pressure flash tank is too high, so that the over-pressure alarm is triggered, reducing the working temperature of the circulating heater to a set working temperature value, and adjusting the opening of the first flow control valve to be minimum;
when the pressure in the negative pressure flash tank is ultrahigh and the alarm of overhigh pressure limit is triggered, the first electric valve is closed so as to cut off feeding, the circulating heater is closed, and the intervention of an operator is waited.
As a preferable scheme, the temperature transmitter in the negative pressure flash tank is provided with an over-low temperature alarm, an over-high temperature alarm and an over-high temperature limit alarm, and when the temperature in the negative pressure flash tank is not within a normal range, and a corresponding alarm is triggered, the alarm is processed in the following manner:
when the temperature in the negative pressure flash tank is lower than 120 ℃, and the over-low temperature alarm is triggered, the circulating heater is adjusted to work under the condition that the heating value is the upper limit value of the set working temperature, so that the solution in the negative pressure flash tank is heated to the set normal range as soon as possible; if the circulating heater works under the condition that the heating value is the set working temperature upper limit value, reducing the opening degree of a first flow control valve on the feeding loop to reduce the feeding flow;
when the temperature in the negative pressure flash tank is too high and the temperature alarm is triggered, reducing the working temperature of the circulating heater to a set working temperature value;
when the temperature in the negative pressure flash tank is ultrahigh and the alarm of the overhigh temperature limit is triggered, the circulating heater is immediately closed to wait for intervention of an operator.
As a preferable scheme, when the density of the MEG barren solution measured in real time by a density indicator in the MEG barren solution receiving tank is smaller than a set lower limit value, checking whether a circulating heater is started and the heating value of the circulating heater is a set working temperature upper limit value, and if the circulating heater is not started or the heating value of the circulating heater does not reach the set working temperature upper limit value, heating the circulating heater to work according to the set working temperature upper limit value so as to accelerate the distillation speed of the saline ethylene glycol barren solution in the negative pressure flash tank; if the circulating heater is started at the moment and the heating capacity of the circulating heater reaches the upper limit value of the set working temperature, reducing the opening degree of a first flow control valve in the feeding loop to be minimum, or closing the first flow control valve on the feeding loop until the purity of the ethylene glycol reaches a preset value, then re-opening the first electric valve, opening the opening degree of the first flow control valve to a normal value, and reducing the heating temperature of the circulating heater to the set working temperature value;
when the density measured by a density indicator of the MEG barren solution in the MEG barren solution receiving tank in real time is smaller than a qualified value, checking whether a circulating heater is started and the heating value of the circulating heater is the upper limit value of the set working temperature, and if the circulating heater is not started or the heating value of the circulating heater does not reach the upper limit value of the set working temperature, enabling the circulating heater to work according to the heating value as the upper limit value of the set working temperature so as to accelerate the distillation speed of the saline ethylene glycol barren solution in the negative pressure flash tank; if the circulating heater is started at the moment and the heating capacity of the circulating heater reaches the upper limit value of the set working temperature at the moment, the opening degree of a first flow control valve in the feeding loop is reduced to reduce the feeding speed drop, and the separation efficiency of the negative pressure flash tank is improved.
The method has the beneficial effects that: the method can ensure that the desalting system finishes the desalting operation of the glycol barren solution containing high-solubility salt in the deep sea natural gas exploitation, and has high glycol recovery rate and safe and reliable operation.
In the step 1-1, in the raw material transportation, the first flow control valve is opened, and the first bypass valve is closed at the same time, so that the saline glycol barren solution raw material with the temperature of about 95 ℃ is conveyed into the negative pressure flash tank, and the impact on the mechanism caused by the direct opening of the valve transportation can be prevented;
in the purification in the step 2-2, because a small amount of uncondensed gas is inevitably mixed with the MEG barren solution gas in the condensation process and is merged into the MEG barren solution receiving tank along with the condensate, a vacuum valve and a pneumatic vacuum pump are opened to discharge a small amount of gas in the MEG barren solution receiving tank;
in the centrifugal separation in the step 3-2, some insoluble gas mixed in the salt solution sent to the centrifugal machine is discharged through a thirteenth one-way valve above the centrifugal machine, after the centrifugation of the residual solid-liquid mixture, solid salt blocks are stored in a salt tank to be stored as a subsequent deep processing raw material, and the residual solution which is not completely centrifuged flows back into the salt solution tank again through a liquid phase outlet of the centrifugal machine, so that the liquid level of the salt solution tank is supplemented, and the solution participates in the centrifugation again to reduce the loss of ethylene glycol;
in step 3-3, once the brine in the brine tank meets the centrifugation requirement, the brine in the brine tank is continuously centrifuged to cause the liquid level in the tank to continuously drop, so that the stability of the whole system can be possibly damaged, when the second liquid level transmitter detects that the liquid level in the brine tank drops to a lower limit value, the second liquid level controller sends a signal, the control system starts a fourth electric valve, water is extracted from the water tank and is injected into the brine tank, and the stability of the liquid level in the brine tank is ensured; and meanwhile, the solution salt concentration in the salt solution tank is reduced by injecting water.
In step 1-4, a first pressure controller and a second pressure transmitter on the negative pressure flash tank ensure that the operating pressure of the negative pressure flash tank is maintained at 15 +/-5 KPa; when the pressure and the temperature in the negative pressure flash tank reach set values, monovalent salt reaches a saturated state in the glycol solution, the saline glycol barren solution starts to carry out flash separation, temperature supplement is carried out through a circulating heating loop to maintain the temperature required in the flash process, the MEG barren solution is distilled out and accumulated at the top of the negative pressure flash tank in a gas phase mode, and the efficiency of flash evaporation desalination is improved.
If the liquid level in the negative pressure flash tank is too high, the solution may immerse a demister arranged at the top of the negative pressure flash tank, so that the demister is corroded to cause the normal work of the solution; if the liquid level is low excessively, it is not enough to indicate that it is not enough to contain salt ethylene glycol barren solution in the negative pressure flash tank, and this normal work that will influence other equipment in the experimental apparatus leads to the whole operating efficiency of experimental system low, influences the experimental result. The method effectively realizes the liquid level control in the negative pressure flash tank.
When the liquid level in the negative pressure flash tank is at a normal level, whether the pressure level therein is normal or not is judged. Thereby ensuring the normal working environment of relevant instruments and equipment and improving the distillation efficiency of the saline glycol barren solution.
When the liquid level and the pressure in the negative pressure flash tank are both at normal levels, whether the temperature level in the negative pressure flash tank is normal or not is judged. Thereby further guaranteeing the normal working environment of relevant instruments and equipment and improving the distillation efficiency of the saline glycol barren solution.
Insufficient purity of ethylene glycol in the MEG lean solution receiving tank can lead to unqualified products, cannot meet the production requirements, and can cause economic loss to the whole ethylene glycol regeneration and recovery system. After the desalination device starts, along with the continuous going on of gas-liquid separation process in the negative pressure flash tank, during the continuous output of the MEG barren solution after the desalination and collected MEG barren solution receiving tank, along with the liquid level in the MEG barren solution receiving tank constantly risees, treat that the liquid level height reaches preset control point, take out the MEG barren solution after the desalination through the third transportation pump, liquid density carries out real-time measurement through the density indicator who installs in the return circuit in the MEG barren solution receiving tank. And when the measured density does not reach the preset limit value, controlling the flow on the feeding loop and the working temperature of the circulating heater, thereby ensuring that the purity of the ethylene glycol in the MEG barren liquor receiving tank is qualified.
Drawings
FIG. 1 is a diagram of a desalination system arrangement according to the present invention.
In fig. 1: 1-a saline ethylene glycol barren solution tank, 2-a first transport pump, 3-a negative pressure flash tank, 4-a second transport pump, 5-a circulating heater, 6-a negative pressure condenser, 7-an MEG barren solution receiving tank, 8-a vacuum pump, 9-a third transport pump, 10-a qualified MEG barren solution storage tank, 11-a water tank, 12-a fourth transport pump, 13-a salt solution tank, 14-a fifth transport pump, 15-a centrifuge and 16-a salt tank;
v1-first stop valve, V2-first bypass valve, V3-first check valve, V4-first electric valve, V5-first flow control valve, V6-second check valve, V7-third check valve, V8-second electric valve, V9-vacuum valve, V10-third stop valve, V11-second bypass valve, V12-fourth check valve, V13-fifth check valve, V14-sixth check valve, V15-seventh check valve, V16-eighth check valve, V17-ninth check valve, V18-third electric valve, V19-fourth stop valve, V20-fourth bypass valve, V21-tenth check valve, V22-fourth electric valve, V23-second flow control valve, V24-fifth stop valve, V25-fifth stop valve, V26-eleventh check valve, v27-fifth electric valve, V28-twelfth one-way valve, V29-sixth electric valve, V30-thirteenth one-way valve, V31-fourteenth one-way valve;
s1-a first pressure transmitter, S2-a first temperature transmitter, S3-a first flow transmitter, S4-a first flow controller, S5-a first pressure controller, S6-a second pressure transmitter, S7-a first pressure gauge, S8-a first level transmitter, S9-a first level controller, S10-a first temperature gauge, S11-a temperature checker, S12-a first differential pressure transmitter, S13-a second temperature transmitter, S14-a second pressure gauge, S15-a third pressure gauge, S16-a first conductivity tester, S17-a third temperature transmitter, S18-a temperature controller, S19-a third pressure transmitter, S20-a second temperature gauge, S21-a level gauge, S22-a fourth pressure transmitter, S23-a fifth pressure transmitter, s24-a third temperature table, S25-a second differential pressure transmitter, S26-a second pressure controller, S27-a fourth temperature table, S28-a fourth temperature transmitter, S29-a fifth temperature table, S30-a sixth temperature table, S31-a fourth pressure table, S32-a second flow transmitter, S33-a second flow controller, S34-a seventh temperature table, S35-a second liquid level transmitter, S36-a second liquid level controller, S37-a fifth pressure table, S38-a second conductivity meter, S39-a sixth pressure transmitter, S40-a third flow transmitter, S41-a third flow controller.
Detailed Description
Specific embodiments of the present invention will be described in detail below with reference to the accompanying drawings.
As shown in fig. 1, a desalination system for glycol barren solution containing high-solubility salt in deep sea natural gas exploitation comprises an MEG barren solution recovery device, a salt-containing glycol barren solution flash evaporation device and a first-order salt recovery device;
the salt-containing glycol lean solution flash evaporation device comprises a salt-containing glycol lean solution tank 1, the salt-containing glycol lean solution tank is connected with a first transport pump 2 through a pipeline, a first stop valve V1 is installed on the pipeline between the salt-containing glycol lean solution tank 1 and the first transport pump 2, a three-way valve is connected to an output port of the first transport pump 2, one of the three-way valve is connected to the pipeline between the salt-containing glycol lean solution tank and a first stop valve V1 through a pipeline provided with a first bypass valve V2 to form a first bypass loop, and a first pressure transmitter S1 is installed on the pipeline between a loop connecting port of the first bypass loop and the first stop valve V1; the first transport pump 2 is connected with the negative pressure flash tank 3 through a pipeline, a first check valve V3, a first electric valve V4 and a first flow control valve V5 are sequentially arranged on the pipeline between the first transport pump 2 and the negative pressure flash tank 3, a first temperature transmitter S2 is arranged on the pipeline between the first transport pump 2 and the check valve V3, a first flow transmitter S3 and a first flow controller S4 are arranged on the pipeline between the electric valve V4 and the flow control valve V5, and the flow in the transport pipe can be adjusted according to information such as pressure, liquid level and temperature in the negative pressure flash tank 3; the negative pressure flash tank is provided with two liquid phase outlets and a gas phase outlet positioned on the top of the tank, the gas phase outlet is communicated with the negative pressure condenser 6 through a pipeline, one liquid phase outlet is connected with the salt solution tank 13 through a downcomer, the other liquid phase outlet is connected with the circulating heater 5 through the second transportation pump 4, and the outlet of the circulating heater 5 is connected with the negative pressure flash tank 3 to form a closed loop;
a first pressure controller S5, a second pressure transmitter S6 and a first pressure gauge S7 which monitor and control the pressure in the negative pressure flash tank 3 in real time are arranged on the negative pressure flash tank 3, a temperature gauge S10 and a temperature check meter S11 are also arranged on the negative pressure flash tank 3, and a first liquid level transmitter S8 and a first liquid level controller S9 which control the lowest liquid level to ensure the stability of the MEG lean liquid amount flashed in the tank are arranged at the lower part of the inner side of the tank body of the negative pressure flash tank 3; a fourth pressure transmitter S22 and a fifth check valve V13 are arranged on a pipeline between the negative pressure flash tank 3 and the second transport pump 4, a sixth check valve V14 and a seventh check valve V15 are arranged on a pipeline between the second transport pump 4 and the circulating heater 5, and a fifth pressure transmitter S23 and a third thermometer S24 are arranged on a pipeline between the sixth check valve V14 and the seventh check valve V15; an outlet of the circulating heater 5 is connected with the negative pressure flash tank 3 through a pipeline provided with an eighth check valve V16, a second pressure difference transmitter S25 is connected between a pipeline at an outlet end of the sixth check valve V14 and a pipeline at an outlet end of the seventh check valve V15, and a second pressure controller S26, a fourth temperature meter S27, a fourth temperature transmitter S28 and a fifth temperature meter S29 which are used for ensuring the temperature of the heated MEG lean liquid and reaching a specified value are arranged on the pipeline between the eighth check valve V16 and the negative pressure flash tank 3.
The MEG recovery system comprises a negative pressure condenser 6 communicated with a negative pressure flash tank 3 through a pipeline provided with a second check valve V6, and a first pressure difference transmitter S12, a second pressure gauge S14 and a second temperature transmitter S13 are arranged on the pipeline between the negative pressure flash tank 3 and the negative pressure condenser 6; the negative pressure condenser 6 is connected with an MEG barren liquor receiving tank 7 through a pipeline provided with a third one-way valve V7 and a second one-way valve V8, a third pressure gauge S15 is arranged between the negative pressure condenser 6 and the third one-way valve V7 on the pipeline, and a first conductivity determinator S16, a third temperature transmitter S17 and a temperature controller S18 which are used for confirming the content of high-solubility monovalent salt ions in MEG barren liquor obtained after flash evaporation are arranged on the pipeline between the second one-way valve V8 and the MEG barren liquor receiving tank 7; the MEG lean liquid receiving tank 7 is provided with a third pressure transmitter S19, a second thermometer S20 and a liquid level meter S21 for monitoring the pressure, the temperature and the liquid level in the tank; the top of the MEG lean liquid receiving tank 7 is provided with a gas phase outlet which is connected with a vacuum pump 8 through a pipeline provided with a vacuum valve V9, a liquid phase outlet at the bottom of the MEG lean liquid receiving tank 7 is connected with a third transport pump 9 through a third stop valve V10, a second bypass valve V11 is connected between the inlet of the third stop valve V10 and the outlet of the third transport pump 9, and the third transport pump 9 is communicated with a qualified MEG lean liquid storage tank 10 through a fourth one-way valve V12.
The monovalent salt recovery system comprises a water tank 11, the water tank 11 is communicated with a salt liquid tank 13 through a pipeline provided with a fourth transportation pump 12, and the fourth transportation pump 12 forms a bypass loop through a pipeline provided with a fourth stop valve V19 and a fourth bypass valve V20; a tenth check valve V21, a fourth electric valve V22 and a second flow control valve V23 are sequentially arranged on a pipeline between the outlet of the fourth transport pump 12 and the salt liquid tank 13; a fourth pressure gauge S31 is arranged on a pipeline between the fourth transportation pump 12 and the one-way valve V21, and a second flow rate transmitter S32 and a second flow rate controller S33 which control the water inflow according to the concentration of the salt solution in the salt solution tank 13 are arranged on a pipeline between the electric valve V22 and the flow rate control valve V23; the negative pressure flash tank 3 is connected with the salt liquid tank 13 through a pipeline which is sequentially provided with a ninth one-way valve V17 and a third electric valve V18, and a seventh temperature gauge S34, a second liquid level transmitter S35, a second liquid level controller S36, a fifth pressure gauge S37 and a second conductivity meter S38 which are used for monitoring the concentration of the salt solution in the salt liquid tank 13 in real time and maintaining the liquid level in the salt liquid tank 13 to be stable are arranged on the salt liquid tank 13;
the tank 13 is connected with a fifth transport pump 14 through two pipelines which are arranged in parallel and provided with a fifth stop valve V24 and a fifth bypass valve V25, an eleventh check valve V26 and a fifth electric valve V27 are connected to the pipeline between the fifth transport pump 14 and the centrifuge 15, a sixth pressure transmitter S39 is arranged on the pipeline between the transport pump 14 and the check valve V26, and a third flow transmitter S40 and a third flow controller S41 are arranged on the pipeline between the fifth electric valve V27 and the centrifuge 15; the centrifugal machine 15 is provided with a gas phase outlet at the top, a solid phase outlet at the bottom and a circulation loop outlet, wherein the gas phase outlet at the top is communicated with the outside through a pipeline provided with a thirteenth one-way valve V30, the solid phase outlet at the bottom is communicated with the salt tank 16 through a pipeline provided with a fourteenth one-way valve V31, and the circulation loop outlet is connected with the salt liquid tank 13 through a pipeline provided with a twelfth one-way valve V28 and a sixth electrically operated valve V29.
The desalting method of the desalting system of the ethylene glycol barren solution containing high-solubility salt in the deep sea natural gas exploitation comprises the following specific steps:
step 1, flashing saline glycol barren solution:
step 1-1, raw material transportation: in the initial state, valves in each system are in a closed state; firstly, opening a first stop valve V1 and a first bypass valve V2, starting a first transport pump 2, detecting that the pressure in a pipe is stable after a bypass loop between a saline glycol lean solution tank 1 and the first transport pump 2 is filled with MEG lean solution by a first pressure transmitter S1, then opening an electric valve V4 through remote control, opening a first flow control valve V5, closing the first bypass valve V2 at the same time, and conveying saline glycol lean solution raw materials at the temperature of about 95 ℃ into a negative pressure flash tank 3, so that the impact on the mechanism caused by directly opening valve transportation can be prevented;
step 1-2, flow control: when the first liquid level transmitter S8 on the negative pressure flash tank 3 detects that the solution in the tank reaches the designated liquid level, the control system controls the first flow control valve V5 on the feeding pipe, the flow in the tank is adjusted, and the liquid level of the negative pressure flash tank 3 is maintained to be stable; if an emergency situation happens suddenly, the first electric valve V4 is directly and remotely closed to prevent the raw materials from flowing in;
step 1-3, cyclic heating: the 95 ℃ saline lean glycol feed liquid can not meet the requirement of flash evaporation in a negative pressure flash tank, so the lean glycol feed liquid needs to be heated. The saline glycol barren solution flowing into the negative pressure flash tank 3 is transferred to the circulating heater 5 through the second transport pump 4 to be heated and flows back to the negative pressure flash tank 3 again, and the temperature check meter S11 and the fourth temperature transmitter S28 on the negative pressure flash tank 3 monitor the temperature in the tank in real time to ensure that the temperature in the tank is stabilized at 140 +/-5 ℃;
step 1-4, flash evaporation: the flash evaporation not only needs the temperature to reach a certain value, but also has the requirement on the pressure, and the first pressure controller S5 and the second pressure transmitter S6 on the negative pressure flash evaporation tank ensure that the operating pressure of the negative pressure flash evaporation tank is kept at 15 +/-5 KPa; when the pressure and the temperature in the negative pressure flash tank reach set values, monovalent salt NaCl reaches a saturated state in the glycol solution, the glycol barren solution containing salt starts to flash, MEG barren solution is distilled out and accumulated on the top of the negative pressure flash tank 3 in a gas phase form after continuous circulating heating, and more than 90% of the solution at the bottom of the negative pressure flash tank 3 is monovalent salt solution;
step 2, MEG barren solution recovery:
step 2-1, condensing MEG barren solution: the MEG barren liquor gas generated by flash evaporation enters a negative pressure condenser through a second one-way valve V6, the temperature of hot steam is rapidly reduced to 40 +/-3 ℃, so that the MEG barren liquor gas is liquefied again, then a second electric valve V8 is opened, and the condensate is converged into an MEG barren liquor receiving tank 7;
step 2-2, purification: because a small amount of uncondensed gas is inevitably mixed with the MEG lean solution gas in the condensation process and is merged into the MEG lean solution receiving tank along with the condensate, the vacuum valve V9 and the pneumatic vacuum pump 9 are opened to discharge a small amount of gas in the MEG lean solution receiving tank, and the residual MEG lean solution is stored into the qualified MEG lean solution storage tank 10 through the third transport pump 9 and is used as an inhibitor in the marine natural development process again;
step 3, monovalent salt recovery:
step 3-1, salt solution storage: the salt solution at the bottom of the negative pressure flash tank 3 obtained in the step 1-4 is conveyed into a salt solution tank 13 through a downcomer, monovalent salt such as NaCl and the like in the salt solution tank 13 reaches a saturated state, crystallization and separation are started, and after the salt concentration in the salt solution tank 13 reaches a set value, which is measured by a second conductivity measuring instrument S38, the salt solution is conveyed into a centrifuge 15 through a fifth conveying pump 14 for centrifugation;
step 3-2, centrifugal separation: the salt solution sent to the centrifuge 15 is mixed with some insoluble gas and discharged through a thirteenth one-way valve V30 above the centrifuge 15, after the residual solid-liquid mixture is centrifuged, the solid salt blocks are stored in a salt tank 16 for storage as the subsequent deep processing raw material, and the residual solution which is not completely centrifuged flows back into the salt solution tank 13 through a liquid phase outlet of the centrifuge again, so that the liquid level of the salt solution tank 13 is supplemented, and the solution participates in the centrifugation again to reduce the loss;
step 3-3, water injection: once the salt solution in the salt solution tank 13 meets the centrifugation requirement, the liquid level in the tank is continuously reduced due to continuous centrifugation, so that the stability of the whole system is possibly damaged, when the second liquid level transmitter S35 detects that the liquid level in the salt solution tank 13 is reduced to a lower limit value, the second liquid level controller S36 sends a signal, the control system starts the fourth electric valve V22, water is extracted from the water tank 11 and injected into the salt solution tank 13, and the stability of the liquid level in the salt solution tank 13 is ensured; and meanwhile, the solution salt concentration in the salt solution tank 13 is reduced by water injection, when the salt concentration in the salt solution tank 13 is lower than a set value as measured by the second conductivity meter S38, the work of the centrifuge 15 is stopped, the fifth electric valve V27 and the fifth transport pump 14 are closed until the next centrifugal processing condition is met, and the step 3-1 is carried out for circulation.
The liquid level in the negative pressure flash tank 3 has set up liquid level limit too high warning, liquid level and has crossed low warning and liquid level limit and cross low warning through liquid level transmitter, when the liquid level is not in normal range, when leading to having triggered above warning, handles according to following mode:
when the liquid level of the saline ethylene glycol barren solution in the negative pressure flash tank 3 is higher than 1450mm and an over-high liquid level limit alarm is triggered, a first electric valve V4 in the feeding loop is cut off to prevent the saline ethylene glycol barren solution from immersing a demister or entering a condenser; thereafter, as the distillation process continues, the liquid level in the negative pressure flash tank 3 is reduced to be lower than 550mm, and when the liquid level is triggered to be too low and an alarm is given, the feeding loop is opened again; effectively prevent that the negative pressure flash tank 3 is interior to contain salt MEG barren liquor submergence defroster or enter into the condenser in, avoided equipment to be corroded, improved system equipment's security, reduced the replacement cycle of the risk of equipment damage and equipment.
When the liquid level in the negative pressure flash tank 3 is lower than 550mm, triggering an alarm of too low liquid level limit, and emergently closing the circulating heater 5 to control the temperature of the saline glycol barren solution in the negative pressure flash tank 3 to be below 170 ℃; after that, the salt-containing glycol barren solution newly injected into the negative pressure flash tank 3 is heated to cause the distillation process to be slow, the liquid level in the negative pressure flash tank 3 is gradually increased, and when the liquid level is too high to trigger the alarm of the liquid level being too high, the circulating heater 5 is restarted; the liquid level in the negative pressure flash tank 3 is prevented from being lower than the circulating outlet pipeline, a protection mechanism is formed, and the safety and the stability of the system are improved.
When the liquid level in the negative pressure flash tank 3 is higher than 1100mm, triggering a liquid level overhigh alarm, checking whether the circulating heater 5 is started and the heating value of the circulating heater is 160 ℃ of the upper limit value of the working temperature, and if the circulating heater 5 is not started or the heating value of the circulating heater is not 160 ℃ of the upper limit value of the working temperature, enabling the circulating heater 5 to work according to the heating value of 160 ℃ of the upper limit value of the working temperature so as to accelerate the distillation speed of the saline glycol barren solution in the negative pressure flash tank 3; if the circulation heater 5 is started at this time and the heating amount of the circulation heater 5 reaches the working temperature upper limit value of 160 ℃ at this time, the opening degree of the first flow control valve V5 in the feeding loop is reduced to reduce the feeding speed; through the liquid level in real-time supervision and the regulation negative pressure flash tank 3, guarantee the dynamic balance of feed flow, improved the separation efficiency in the negative pressure flash tank 3, reduce the system energy consumption.
When the liquid level in the negative pressure flash tank 3 is lower than 700mm, triggering a liquid level over-low alarm, and adjusting the opening degree of a first flow control valve V5 in the feeding loop to be maximum; if the feeding flow is maximum, the working temperature of the circulating heater 5 is reduced to a set working temperature value of 140-150 ℃, so that the distillation speed is reduced.
The pressure transmitter on the upper part of the negative pressure flash tank 3 is provided with an over-high pressure alarm, an over-low pressure alarm and an over-high pressure limit alarm, and when the pressure in the negative pressure flash tank 3 is not in a normal range, corresponding alarm is triggered, and the pressure transmitter is processed in the following mode:
when the pressure in the upper limit value of the working temperature of the negative pressure flash tank 3 is lower than 0.008MPa, and the alarm of too low pressure is triggered, increasing the working temperature of the circulating heater 5 to 160 ℃ as the upper limit value of the working temperature;
when the pressure in the negative pressure flash tank 3 is higher than 0.05MPa, and the over-pressure alarm is triggered, reducing the working temperature of the circulating heater 5 to a set working temperature value of 140 ℃, and adjusting the opening degree of the first flow control valve V5 to be minimum;
when the pressure in the negative pressure flash tank 3 is higher than 0.2MPa and the alarm of the overhigh pressure limit is triggered, the first electric valve V4 is closed to cut off feeding, and the circulating heater 5 is closed to wait for intervention of an operator.
The dynamic balance of the pressure in the negative pressure flash tank 3 is realized, and the energy consumption of the circulating heater 5 is reduced.
The temperature transmitter in the negative pressure flash tank 3 sets the alarm of the over-low temperature, the alarm of the over-high temperature and the alarm of the over-high temperature limit, and when the temperature in the negative pressure flash tank 3 is not in the normal range, the corresponding alarm is triggered, and the temperature transmitter is processed according to the following mode:
when the temperature in the negative pressure flash tank 3 is lower than 120 ℃, and an over-low temperature alarm is triggered, the circulating heater 5 is adjusted to work under the condition that the heating value is 160 ℃ as the set working temperature upper limit value, so that the solution in the flash tank is heated to 140-150 ℃ as soon as possible; if the circulation heater 5 has been operated with the heating value being 160 deg.C as the set operating temperature upper limit value, the opening degree of the first flow rate control valve V5 on the feed circuit is reduced to reduce the feed flow rate to 15m3H; the temperature in the negative pressure flash tank 3 is monitored in real time, and temperature supplement is carried out in time when the temperature is reduced, so that full implementation of flash evaporation is ensured, the efficiency of flash evaporation separation is improved, and the product quality of the recovered MEG barren solution in the system is improved.
When the temperature in the negative pressure flash tank 3 is higher than 150 ℃, and an over-temperature alarm is triggered, reducing the working temperature of the circulating heater 5 to a set working temperature value of 140 ℃; the temperature is prevented from being overhigh, the heat load of the system is effectively reduced, and the energy consumption is reduced on the premise of ensuring the recovery rate of the ethylene glycol.
When the temperature in the negative pressure flash tank 3 is higher than 170 ℃, and the alarm of the overhigh temperature limit is triggered, the circulating heater 5 is immediately closed to wait for the intervention of an operator. Effectively prevents the thermal decomposition of the glycol due to the temperature exceeding the thermal decomposition temperature, and improves the recovery rate of the glycol barren solution in the system.
1.03X 10 when the density of MEG lean liquid measured in real time by the density indicator in the MEG lean liquid receiving tank 7 is less than a set lower limit value3kg/m3Checking whether the circulating heater 5 is started and the heating value of the circulating heater is 160 ℃ of the set working temperature upper limit value, and if the circulating heater 5 is not started or the heating value of the circulating heater is not 160 ℃ of the set working temperature upper limit value, heating the circulating heater 5 to 160 ℃ of the set working temperature upper limit value to work so as to accelerate the distillation speed of the saline ethylene glycol barren solution in the negative pressure flash tank 3; if the circulation heater 5 is started at the moment, and the heating amount of the circulation heater 5 reaches the set working temperature upper limit value of 160 ℃, reducing the opening degree of the first flow control valve V5 in the feeding loop to be minimum, or closing the first flow control valve V5 on the feeding loop until the purity of the ethylene glycol reaches the preset value of 1.1 multiplied by 103kg/m3Opening the first electric valve V4 again, opening the opening degree of the first flow control valve V5 to a normal value, and reducing the heating temperature of the circulating heater 5 to a set working temperature value of 140-150 ℃;
1.1 × 10 when the density of the MEG lean liquid in the MEG lean liquid receiving tank 7 measured in real time by the density indicator is less than the acceptable value3kg/m3Checking whether the circulating heater 5 is started and the heating value of the circulating heater is 160 ℃ of the set working temperature upper limit value, and if the circulating heater 5 is not started or the heating value of the circulating heater is not 160 ℃ of the set working temperature upper limit value, enabling the circulating heater 5 to work according to the heating value of 160 ℃ of the set working temperature upper limit value so as to accelerate the distillation speed of the saline ethylene glycol barren solution in the negative pressure flash tank 3; if the circulating heater 5 is started at the moment and the heating quantity of the circulating heater 5 reaches the set working temperature upper limit value of 160 ℃ at the moment, reducingThe opening degree of a first flow control valve V5 in the feeding loop is used for reducing the feeding speed drop and improving the separation efficiency of the negative pressure flash tank 3;
the above-mentioned embodiments are merely illustrative of the principles and effects of the present invention, and some embodiments may be used, not restrictive; it should be noted that, for those skilled in the art, various changes and modifications can be made without departing from the inventive concept of the present invention, and these changes and modifications belong to the protection scope of the present invention.

Claims (11)

1. A desalination system of ethylene glycol barren liquor containing high-solubility salt in deep sea natural gas exploitation is characterized in that: the method comprises an MEG barren solution recovery device, a salt-containing glycol barren solution flash evaporation device and a first-order salt recovery device;
the device comprises a salt-containing glycol barren solution flash device, a first transportation pump, a first check valve, a first electric valve and a first flow control valve, wherein the salt-containing glycol barren solution flash device is connected with the first transportation pump through a pipeline, the first transportation pump is connected with a negative pressure flash tank through a pipeline, the pipeline between the first transportation pump and the negative pressure flash tank is sequentially provided with the first check valve, the first electric valve and the first flow control valve, the pipeline between the first transportation pump and the check valve is provided with a first temperature transmitter, the pipeline between the electric valve and the flow control valve is provided with a first flow transmitter and a first flow controller, the negative pressure flash tank is provided with two liquid phase outlets and a gas phase outlet positioned at the top of the tank, the gas phase outlet is communicated with the negative pressure condenser through a pipeline, one of the liquid phase outlets is connected with the salt solution tank through a downcomer, the other of the liquid phase outlets is connected with a circulating heater through a second transportation pump, and the outlet of the The flash tank forms a closed loop;
a first pressure controller, a second pressure transmitter and a first pressure gauge which are used for monitoring and controlling the pressure in the negative pressure flash tank in real time are arranged on the negative pressure flash tank, a thermometer and a temperature check meter are also arranged on the negative pressure flash tank, a fourth pressure transmitter and a fifth one-way valve are arranged on a pipeline between the negative pressure flash tank and the second transport pump, a sixth one-way valve and a seventh one-way valve are arranged on a pipeline between the second transport pump and the circulating heater, and a fifth pressure transmitter and a third thermometer are arranged on a pipeline between the sixth one-way valve and the seventh one-way valve; an outlet of the circulating heater is connected with the negative pressure flash tank through a pipeline provided with an eighth one-way valve, and a second pressure controller, a fourth thermometer, a fourth temperature transmitter and a fifth thermometer which are used for ensuring the temperature of the heated MEG barren solution and reaching a specified value are arranged on the pipeline between the eighth one-way valve and the negative pressure flash tank;
the salt-containing glycol barren solution flash evaporation device comprises a negative pressure condenser communicated with a negative pressure flash evaporation tank through a pipeline provided with a second one-way valve, and a first pressure difference transmitter, a second pressure gauge and a second temperature transmitter are arranged on the pipeline between the negative pressure flash evaporation tank and the negative pressure condenser; the negative pressure condenser is connected with the MEG barren liquor receiving tank through a pipeline provided with a third one-way valve and a second electrically operated valve, a third pressure gauge is arranged between the negative pressure condenser and the third one-way valve on the pipeline, and a first conductivity tester, a third temperature transmitter and a temperature controller are arranged on the pipeline between the second electrically operated valve and the MEG barren liquor receiving tank and used for confirming the content of high-solubility monovalent salt ions in MEG barren liquor obtained after flash evaporation; the MEG lean solution receiving tank is provided with a third pressure transmitter, a second thermometer and a liquid level meter; a gas-phase outlet arranged at the top of the MEG lean solution receiving tank is connected with a vacuum pump through a pipeline provided with a vacuum valve, a liquid-phase outlet at the bottom of the MEG lean solution receiving tank is connected with a third transport pump through a third stop valve, a second bypass valve is connected between an inlet of the third stop valve and an outlet of the third transport pump, and the third transport pump is communicated with a qualified MEG lean solution storage tank through a fourth one-way valve;
the monovalent salt recovery system comprises a water tank, the water tank is communicated with the salt liquid tank through a pipeline provided with a fourth transport pump, and a tenth check valve, a fourth electric valve and a second flow control valve are sequentially arranged on the pipeline between an outlet of the fourth transport pump and the salt liquid tank; a fourth pressure gauge is arranged on a pipeline between the fourth transportation pump and the one-way valve, and a second flow transmitter and a second flow controller for controlling the water inflow according to the concentration of the salt solution in the salt solution tank are arranged on a pipeline between the electric valve and the flow control valve; the negative pressure flash tank is connected with the salt liquid tank through a pipeline which is sequentially provided with a ninth one-way valve and a third electric valve, and a seventh thermometer, a second liquid level transmitter, a second liquid level controller, a fifth pressure gauge and a second conductivity tester which are used for monitoring the concentration of the salt solution in the salt liquid tank in real time and maintaining the liquid level in the salt liquid tank to be stable are arranged on the salt liquid tank;
the salt solution tank is respectively connected with a fifth transport pump through a pipeline provided with a fifth stop valve and a pipeline of a fifth bypass valve which are arranged in parallel, an eleventh one-way valve and a fifth electric valve are connected to the pipeline between the fifth transport pump and the centrifugal machine, a sixth pressure transmitter is arranged on the pipeline between the transport pump and the one-way valve, and a third flow transmitter and a third flow controller are arranged on the pipeline between the fifth electric valve and the centrifugal machine; the centrifugal machine is provided with a gas phase outlet positioned at the top and a solid phase outlet positioned at the bottom, wherein the gas phase outlet positioned at the top is communicated with the outside through a pipeline provided with a thirteenth one-way valve, and the solid phase outlet positioned at the bottom is communicated with the salt tank through a pipeline provided with a fourteenth one-way valve.
2. The system for desalting ethylene glycol barren solution containing high-solubility salt in deep sea natural gas extraction according to claim 1, wherein: and the output port of the first transport pump is also connected to a pipeline between the saline glycol lean solution tank and the first stop valve through a pipeline provided with a first bypass valve to form a first bypass loop, and a first pressure transmitter is arranged on a pipeline between a loop connecting port of the first bypass loop and the first stop valve.
3. The system for desalting ethylene glycol barren solution containing high-solubility salt in deep sea natural gas extraction according to claim 1, wherein: the lower part of the inner side of the tank body of the negative pressure flash tank is provided with a first liquid level transmitter and a first liquid level controller which are used for controlling the lowest liquid level so as to ensure the stable MEG lean liquor amount of flash evaporation in the tank.
4. The system for desalting ethylene glycol barren solution containing high-solubility salt in deep sea natural gas extraction according to claim 1, wherein: and a second differential pressure transmitter is connected between the pipeline at the outlet end of the sixth one-way valve and the pipeline at the outlet end of the seventh one-way valve.
5. The system for desalting ethylene glycol barren solution containing high-solubility salt in deep sea natural gas extraction according to claim 1, wherein: and the fourth transport pump forms a bypass loop through a pipeline provided with a fourth stop valve and a fourth bypass valve.
6. The system for desalting ethylene glycol barren solution containing high-solubility salt in deep sea natural gas extraction according to claim 1, wherein: and the centrifugal machine is provided with a bottom circulation loop outlet, and the circulation loop outlet is connected with the salt solution tank through a pipeline provided with a twelfth one-way valve and a sixth electric valve.
7. The desalination method of the ethylene glycol barren solution containing high-solubility salt in the deep sea natural gas exploitation as claimed in any one of claims 1-6, which comprises the following specific steps:
step 1, flashing saline glycol barren solution:
step 1-1, raw material transportation: in the initial state, valves in each system are in a closed state; the method comprises the steps that firstly, a first stop valve and a first bypass valve are opened, a first transport pump is started, when a bypass loop between a saline ethylene glycol lean solution tank and the first transport pump is filled with MEG lean solution, a first pressure transmitter detects that the pressure in the pipe is stable, then an electric valve is opened through remote control, a first flow control valve is opened, meanwhile, the first bypass valve is closed, and the saline ethylene glycol lean solution raw material is conveyed into a negative pressure flash tank;
step 1-2, flow control: when a first liquid level transmitter on the negative pressure flash tank detects that the solution in the tank reaches a specified liquid level, a first flow control valve on a feeding pipe is controlled through a control system, the flow in the tank is adjusted, and the liquid level of the negative pressure flash tank is maintained to be stable; if an emergency situation occurs suddenly, the first electric valve is directly and remotely closed to prevent the raw materials from flowing in;
step 1-3, cyclic heating: the saline ethylene glycol barren solution flowing into the negative pressure flash tank is transferred to a circulating heater through a second transport pump to be heated and flows back to the negative pressure flash tank again, and a temperature calibrator and a fourth temperature transmitter on the negative pressure flash tank monitor the temperature in the tank in real time to ensure that the temperature in the tank is stabilized at 140 +/-5 ℃;
step 1-4, flash evaporation: the first pressure controller and the second pressure transmitter on the negative pressure flash tank ensure that the operating pressure of the negative pressure flash tank is kept at 15 +/-5 KPa; due to the reduction of the pressure, the ethylene glycol in the negative pressure flash tank starts to carry out flash separation, the temperature supplement is carried out through the circulating heating loop to maintain the temperature required in the flash process, and MEG barren solution is distilled out and accumulated at the top of the negative pressure flash tank in a gas phase form;
step 2, MEG barren solution recovery:
step 2-1, condensing MEG barren solution: the MEG barren liquor gas generated by flash evaporation enters a negative pressure condenser through a second one-way valve, so that the temperature of hot steam is rapidly reduced to 40 +/-3 ℃ to reliquefy the MEG barren liquor gas, then a second electric valve is opened, and the condensate is converged into an MEG barren liquor receiving tank;
step 2-2, purification: opening a vacuum valve and a pneumatic vacuum pump, discharging a small amount of gas in the MEG lean liquid receiving tank, and storing the residual MEG lean liquid into a qualified MEG lean liquid storage tank through a third transport pump;
step 3, monovalent salt recovery:
step 3-1, salt solution storage: the salt solution at the bottom of the negative pressure flash tank obtained in the step 1-4 is conveyed into a salt solution tank through a downcomer, monovalent salt in the salt solution tank reaches a saturated state, crystallization and separation are started, and after the salt concentration in the salt solution tank reaches a set value measured by a second conductivity measuring instrument, the salt solution is conveyed into a centrifuge through a fifth conveying pump for centrifugation;
step 3-2, centrifugal separation: the brine sent to the centrifuge is mixed with some insoluble gas and discharged through a thirteenth one-way valve above the centrifuge, after the residual solid-liquid mixture is centrifuged, the solid salt blocks are stored in a salt tank to be used as the raw material for subsequent deep processing, and the residual solution which is not completely centrifuged flows back into the brine tank through a liquid phase outlet of the centrifuge again;
step 3-3, water injection: when the second liquid level transmitter detects that the liquid level in the brine tank drops to a lower limit value, the second liquid level controller sends a signal, the control system starts the fourth electric valve, water is extracted from the water tank and injected into the brine tank, and the stability of the liquid level in the brine tank is ensured; and when the second conductivity tester detects that the salt concentration in the salt solution tank is lower than a set value, stopping the operation of the centrifuge, closing the fifth electric valve and the fifth transport pump until the next centrifugal treatment condition is met, and turning to the step 3-1 for circulation.
8. The method for desalting in a desalination system of ethylene glycol barren solution containing high solubility salt in deep sea natural gas extraction according to claim 7, wherein: the liquid level in the negative pressure flash tank has set up liquid level limit too high warning, liquid level and has crossed low warning and liquid level limit and cross low warning through liquid level transmitter, when the liquid level is not in normal range, when leading to having triggered above warning, handles according to following mode:
when the liquid level of the salt-containing glycol barren solution in the negative pressure flash tank is too high and a liquid level limit too high alarm is triggered, a first electric valve in the feeding loop is cut off to prevent the salt-containing glycol barren solution from immersing a demister or entering a condenser; then, with the continuation of the distillation process, when the liquid level in the negative pressure flash tank is reduced to trigger the alarm of too low liquid level, the feeding loop is opened again;
when the liquid level in the negative pressure flash tank is too low and the liquid level limit is too low to alarm, the circulating heater is closed emergently to control the temperature of the saline glycol barren solution in the negative pressure flash tank to be below 170 ℃; after that, the salt-containing glycol barren solution newly injected into the negative pressure flash tank is slowly distilled due to insufficient heating, the liquid level in the negative pressure flash tank is gradually increased, and when the liquid level is too high, the alarm is triggered, the circulating heater is restarted;
when the liquid level in the negative pressure flash tank is too high, triggering a liquid level overhigh alarm, checking whether a circulating heater is started and the heating value of the circulating heater is the working temperature upper limit value, and if the circulating heater is not started or the heating value of the circulating heater does not reach the working temperature upper limit value, enabling the circulating heater to work according to the heating value as the working temperature upper limit value so as to accelerate the distillation speed of the saline ethylene glycol barren solution in the negative pressure flash tank; if the circulating heater is started at the moment and the heating capacity of the circulating heater reaches the working temperature upper limit value at the moment, reducing the opening degree of a first flow control valve in the feeding loop to reduce the feeding speed;
triggering a liquid level over-low alarm when the liquid level in the negative pressure flash tank is over-low, and adjusting the opening of a first flow control valve in a feeding loop to be maximum; if the feeding flow is maximum, the working temperature of the circulating heater is reduced to the set working temperature value, so that the distillation speed is reduced.
9. The method for desalting in a desalination system of ethylene glycol barren solution containing high solubility salts in deep sea natural gas extraction according to claim 8, wherein: the pressure transmitter on the upper part of the negative pressure flash tank is provided with an over-high pressure alarm, an over-low pressure alarm and an over-high pressure limit alarm, and when the pressure in the negative pressure flash tank is not in a normal range and causes the triggering of a corresponding alarm, the pressure transmitter is processed in the following mode:
when the pressure in the working temperature upper limit value of the negative pressure flash tank is too low and the pressure too low alarm is triggered, increasing the working temperature of the circulating heater to the working temperature upper limit value;
when the pressure in the negative pressure flash tank is too high, so that the over-pressure alarm is triggered, reducing the working temperature of the circulating heater to a set working temperature value, and adjusting the opening of the first flow control valve to be minimum;
when the pressure in the negative pressure flash tank is ultrahigh and the alarm of overhigh pressure limit is triggered, the first electric valve is closed so as to cut off feeding, the circulating heater is closed, and the intervention of an operator is waited.
10. The method for desalination in a desalination system of ethylene glycol barren solution containing high solubility salts in deep sea natural gas extraction according to claim 9, characterized in that: the temperature transmitter in the negative pressure flash tank is provided with the alarm for over-low temperature, the alarm for over-high temperature and the alarm for over-high temperature limit, and when the temperature in the negative pressure flash tank is not in a normal range, the corresponding alarm is triggered, and the temperature transmitter is processed according to the following mode:
when the temperature in the negative pressure flash tank is lower than 120 ℃, and the over-low temperature alarm is triggered, the circulating heater is adjusted to work under the condition that the heating value is the upper limit value of the set working temperature, so that the solution in the negative pressure flash tank is heated to the set normal range as soon as possible; if the circulating heater works under the condition that the heating value is the set working temperature upper limit value, reducing the opening degree of a first flow control valve on the feeding loop to reduce the feeding flow;
when the temperature in the negative pressure flash tank is too high and the temperature alarm is triggered, reducing the working temperature of the circulating heater to a set working temperature value;
when the temperature in the negative pressure flash tank is ultrahigh and the alarm of the overhigh temperature limit is triggered, the circulating heater is immediately closed to wait for intervention of an operator.
11. The method for desalting in a desalination system of ethylene glycol barren solution containing high solubility salt in deep sea natural gas extraction according to claim 7, wherein:
when the density of the MEG barren solution measured in real time by a density indicator in the MEG barren solution receiving tank is smaller than a set lower limit value, checking whether a circulating heater is started and the heating value of the circulating heater is a set working temperature upper limit value, and if the circulating heater is not started or the heating value of the circulating heater does not reach the set working temperature upper limit value, heating the circulating heater to work according to the set working temperature upper limit value so as to accelerate the distillation speed of the saline ethylene glycol barren solution in the negative pressure flash tank; if the circulating heater is started at the moment and the heating capacity of the circulating heater reaches the upper limit value of the set working temperature, reducing the opening degree of a first flow control valve in the feeding loop to be minimum, or closing the first flow control valve on the feeding loop until the purity of the ethylene glycol reaches a preset value, then re-opening the first electric valve, opening the opening degree of the first flow control valve to a normal value, and reducing the heating temperature of the circulating heater to the set working temperature value;
when the density measured by a density indicator of the MEG barren solution in the MEG barren solution receiving tank in real time is smaller than a qualified value, checking whether a circulating heater is started and the heating value of the circulating heater is the upper limit value of the set working temperature, and if the circulating heater is not started or the heating value of the circulating heater does not reach the upper limit value of the set working temperature, enabling the circulating heater to work according to the heating value as the upper limit value of the set working temperature so as to accelerate the distillation speed of the saline ethylene glycol barren solution in the negative pressure flash tank; if the circulating heater is started at the moment and the heating capacity of the circulating heater reaches the upper limit value of the set working temperature at the moment, the opening degree of a first flow control valve in the feeding loop is reduced to reduce the feeding speed drop, and the separation efficiency of the negative pressure flash tank is improved.
CN202011029882.6A 2020-09-27 2020-09-27 Desalination system and desalination method for ethylene glycol barren solution containing high-solubility salt in deep sea natural gas exploitation Pending CN112121452A (en)

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