RU2694771C1 - Method of heat recovery of waste process fluids - Google Patents

Method of heat recovery of waste process fluids Download PDF

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Publication number
RU2694771C1
RU2694771C1 RU2019101123A RU2019101123A RU2694771C1 RU 2694771 C1 RU2694771 C1 RU 2694771C1 RU 2019101123 A RU2019101123 A RU 2019101123A RU 2019101123 A RU2019101123 A RU 2019101123A RU 2694771 C1 RU2694771 C1 RU 2694771C1
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Russia
Prior art keywords
distillate
evaporator
liquid
supplied
waste
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RU2019101123A
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Russian (ru)
Inventor
Владимир Александрович Будник
Марат Ринатович Смаков
Александр Сергеевич Кондратьев
Роман Игоревич Бобровский
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Общество с ограниченной ответственностью "ХАММЕЛЬ"
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Priority to RU2019101123A priority Critical patent/RU2694771C1/en
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D1/00Evaporating
    • B01D1/22Evaporating by bringing a thin layer of the liquid into contact with a heated surface
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10MLUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M175/00Working-up used lubricants to recover useful products ; Cleaning

Abstract

FIELD: oil and gas industry.SUBSTANCE: invention relates to petrochemical and gas industry, in particular to methods of separation and purification of waste process fluids, such as glycols, motor, turbine and transformer oils. Method of thermal regeneration of waste process fluids involves feeding liquid into the upper part of the film evaporator. Flue gases from the burner are fed into the annular space of the evaporator. Fluid flows in form of film along inner surface of evaporator into bottom part of evaporator, where there are also vapors and unevaporated liquid residues. Bottom liquid is mixed with bottom-hole liquid of reinforcing column, in which heavy components are condensed due to interaction with distillate flowing from nozzle of reinforcing column. Distillate is supplied by irrigation into upper part of reinforcing column. Distillate is obtained from non-condensed vapors by cooling in a cooler, from where it is supplied into a distillate collecting tank. Distillate is also directed into the upper part of the film evaporator for its repeated purification. Heavy components distillates are extracted from bottom part of film evaporator and bottom part of reinforcing column. After mixing of heavy products of bottom part of film evaporator in pipeline and column reinforcing flow is separated. Most part of obtained flow of heavy products is supplied by pump for mixing with waste liquid supplied for regeneration, and then mixture is supplied to upper part of film evaporator, providing internal circulation of heavy products. Smaller portion of the flow, which is a balance excess of heavy products, is removed from the system. Vacuum pump creates negative pressure in container with distillate.EFFECT: invention provides low pressure in the regeneration unit in range of 1_6–30 kPa, reduces the process temperature to 200–350 °C and prevent temperature decomposition of cleaned liquids.1 cl, 1 dwg

Description

The invention relates to the petrochemical and gas industry, in particular, to methods for the separation and purification of waste process fluids, such as glycols, motor, turbine and transformer oils.
Waste oils and glycols contain products of thermal decomposition and oxidation of oils and additives, products of incomplete combustion of fuel, particles of soot and coke deposits, metal particles from the surface of rubbing parts, water and various mechanical impurities. This creates great technological difficulties in the process of regeneration of these fluids.
A known method of cleaning waste motor oil and installation for its implementation (application for the grant of a patent of the Russian Federation 94037575, IPC B01D 36/00, publ. 07.27.1996,). In this method, the cleaning is carried out by evaporation of low-boiling fractions from a heated thin film of water-oil emulsion, which is prepared at a ratio of 1: 0.5-10, and the oil film is turbulized on a heating surface in a vacuum.
The disadvantages of this method are:
- the use of a significant amount of water, the evaporation of which requires a large expenditure of energy;
- the impossibility of separation from oil of non-volatile macromolecular compounds and colloidal particles of different nature, present in the waste oils;
- use in the design of the installation of the rotor rotating in vacuum and elevated temperature, since coking of the heated surface of the chamber walls and the deposition of solid impurities on the rotor blades leads to a decrease in the thickness of the oil film and failure of the evaporator.
The known method of regeneration of waste industrial oils (RF patent No. 2326934, IPC B01D 1/22, С10М 175/00, publ. 06/20/2008), including heating the oil with saturated steam to at least 100-205 ° С with the formation of a vapor-gas mixture containing a drop of oil mist and a pair of low-boiling fractions. Vapor of a hot film of oil flowing along the inner surface of a pipe in a heated film evaporator is condensed into oil mist in a countercurrent of cold air, after which the oil drops are separated from the air stream saturated with oil mist in the oil separator-impactor by sequential stepwise expansion-compression of the stream pair of elements "nozzle-flap".
The disadvantage of this technical solution is limited functionality, because cannot be used to regenerate glycols.
There is a method of regeneration of a saturated solution of glycol (RF patent No. 2257945, IPC B01D 53/14, B01D 53/26, B01D 3/00 publ. 10.08.2005), including preheating it, taking a solution of glycol from the bottom of the mass transfer column, heating it in the evaporator, feeding the vapor phase formed in the evaporator to the lower part of the column, irrigating it in the upper part of the column and withdrawing the regenerated glycol from the evaporator. The glycol solution supplied for regeneration is divided into at least two parts, one of which is fed to the vaporization of the column top without heating and then to the evaporator, and the remainder is heated and fed directly to the evaporator.
The disadvantage of this method is to reduce the efficiency of the system when using the intermediate coolant - water vapor, which is problematic for installations located in the Far North. Also to the disadvantages of the method is bubble boiling of glycol on the surface of the evaporator tubes, which leads to the deposition of salts on the tubes of heat exchangers.
The objective of the invention is to expand the functionality due to the use for the regeneration of various environments.
The technical result of the invention is to increase the efficiency of regeneration of waste process fluids with an increase in the yield and purity of the purified target products.
The problem is solved and the technical result is achieved by a method of thermal regeneration of waste process fluids, including the supply of liquid to the upper part of the film evaporator, into the annular space of which the flue gases from the burner are fed to preheat the evaporator heat exchanger tubes, allowing the liquid to flow down in the form of a film along their inner surface to the bottom part the evaporator, which also receives vapors and residues of non-evaporated liquid, then the bottom liquid is mixed with the bottom liquid of the strengthening columns in which heavy components are condensed due to interaction with the distillate flowing down from the packing of the strengthening column, which is fed as irrigation into the upper part of the strengthening column, and the distillate is obtained from non-condensed vapors by cooling in a refrigerator, from where it is sent to a tank for collecting distillate, from which the distillate is also sent to the upper part of the film evaporator to re-clean it, with the resultant light components resulting from the distillation These products are removed from the bottom of the film evaporator and the bottom of the strengthening column, and after mixing in the pipeline, most of the feed is supplied by a pump for mixing with the waste liquid supplied for regeneration, and the mixture is fed to the top of the film evaporator, thus providing less internal circulation of heavy products. component of the balance of heavy products, is removed from the system, and a vacuum pump creates a vacuum in the tank with distillate, providing a reduced pressure in hold is reached for regeneration in the range (1,6-30) kPa, reducing the process temperature to 200-350 ° C and the temperature processes to prevent degradation of the cleaning liquid.
The technical result of the invention is achieved by ensuring the technological process under reduced pressure and, accordingly, the operation of the evaporator and the strengthening column at a low temperature. This allows you to minimize the process of thermal destruction of the cleaned liquids and improve the quality of their cleaning.
The invention is illustrated by the schematic diagram of the installation for implementing the method of thermal regeneration of waste process fluids.
The installation contains a pipeline evaporator 1 connected by a piping system, a strengthening column 2 with a nozzle 3, a burner 4, a chimney 5, a refrigerator 6, a container for collecting distillate 7, a vacuum pump 8, the first and second feed pumps, respectively 9 and 10. The burner is connected by a pipeline 11 with the annular space of the evaporator, the bottom part of which is connected by pipe 12 to the bottom part of the reinforcing column 2, the top of which by pipe 13 is connected to a cooler 6, the output of which by pipe 14 is connected to a tank 7 for collecting disti llyat The bottoms of the film evaporator and the strengthening column are connected by pipeline 15 through the first feed pump 9 to the pipeline 16 for feeding heavy (s) products for mixing with the liquid supplied for processing and with pipeline 17 for withdrawing a part of these products from the installation. The mixture of raw materials and heavy products (resins) by pipeline 18 is supplied to the upper part of the film evaporator 1. The bottom of the tank 7 for collecting distillate through the second feed pump 10 is connected through the pipe 19 to the upper part of the strengthening column 2 and through the pipeline 20 to the upper part of the film evaporator 1, in addition, pipeline 21 - with the conclusion of the balance of distillate surplus (purified product).
The method is as follows.
Raw materials (waste process fluids) are mixed with a recirculating flow of heavy products supplied by the first pump 9 from the bottoms of the film evaporator 1 and the strengthening column 2 and through the pipeline 18 are fed to the upper part of the film evaporator 1, where they flow as a film on the inner surface of heat exchange tubes evaporator. To heat the heat exchanging tubes of the film evaporator 1, flue gases from the burner 4 are fed through conduit 11 into the annular space of the evaporator, and the flue gases that have given off their heat are sent to the chimney 5 for release to the atmosphere. The volatile components of the feedstock evaporate and, together with residues of non-evaporated liquid, enter the cube of the evaporator 1, where the vapors are separated from the liquid by separation. Next, through the pipeline 12 they are sent to the bottom part of the strengthening column 2, where they meet with the liquid flowing down from the nozzle 3, which causes condensation of heavy components. Non-condensed vapors from the top of the column 2 through the pipeline 13 is sent to the refrigerator 6, where as a result of cooling they condense and through the pipeline 14 they are withdrawn into the tank 7 to collect the distillate. From the tank 7, the distillate by the second pump 10 is fed via pipeline 19 as irrigation to the upper part of the strengthening column 2, and the distillate surplus is discharged from the installation via pipeline 21. Also the distillate is fed via pipeline 20 to the upper part of the film evaporator to carry out its repeated cleaning in case "Overshoot" of heavy components (resins). The heavy products (resins) resulting from the stripping of light components are withdrawn from the bottom of the film evaporator 1 and the bottom of the strengthening column 2, through line 15, where they are mixed. Further, most of them are pumped by the first pump 9 through pipeline 16 for mixing with fresh raw materials. The mixture of raw materials and heavy products through the pipeline 18 is directed to the upper part of the film evaporator 1, thus forming a circuit for the internal circulation of heavy products (resins). The smaller part, which constitutes the balance of the excess heavy products (resins), is removed from the installation through the pipeline 17.
To increase the efficiency, the regeneration process is carried out under reduced pressure in the range (1.6-30) kPa. To do this, using a vacuum pump 8 installed in the upper part of the tank 7 for collecting distillate create a vacuum. This allows to reduce the operating temperature in the film evaporator 1 and in the strengthening column 2 to 200-350 ° C and prevent the processes of temperature destruction of the liquids being cleaned and, accordingly, improve the quality of their cleaning.
Thus, the proposed invention extends the functionality of the method of regeneration of waste process fluids due to its use for the processing of both glycols and technical oils, and also improves the efficiency of regeneration and the quality of the liquids being cleaned.

Claims (1)

  1. The method of thermal regeneration of waste process fluids, including the supply of liquid to the upper part of the film evaporator, in the annular space of which flue gases are fed from the burner to preheat the heat exchanger tubes of the evaporator, allowing the liquid to flow down in the form of a film along their inner surface to the bottom of the evaporator, which also receives pairs and the remains of non-evaporated liquid, then the bottom liquid is mixed with the bottom liquid of the strengthening column, in which the heavy components are condensed Thanks to the interaction with the distillate flowing down from the nozzle of the strengthening column, which is fed as irrigation to the upper part of the strengthening column, the distillate is obtained from non-condensed vapors by cooling in a refrigerator, from where it is sent to the distillate collection tank, from which the distillate is also sent to the upper part film evaporator to re-clean it, while the resultant light components resulting from the stripping of light components are removed from the bottom of the film After mixing in the pipeline, most part is supplied by a pump for mixing with the waste liquid supplied for regeneration, and the mixture is fed to the upper part of the film evaporator, thus providing for the internal circulation of heavy products, and a smaller, balance component of heavy products, out of the system, and creating a vacuum pump vacuum in the tank with distillate, providing reduced pressure in the unit for regeneration in the range of 1.6-30 kPa, which allows It can reduce the process temperature to 200-350 ° С and prevent the processes of temperature destruction of the liquids being cleaned.
RU2019101123A 2019-01-14 2019-01-14 Method of heat recovery of waste process fluids RU2694771C1 (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2728970C1 (en) * 2020-02-04 2020-08-03 Общество с ограниченной ответственностью "НефтеХимКонсалт" Method of two-stage thermal regeneration of waste industrial fluids

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3738391A1 (en) * 1987-11-12 1989-05-24 Wilhelm Joachim A Dr Ing Process for removing impurities by distillation from used oil
US4894140A (en) * 1986-11-12 1990-01-16 Schoen Christian O Method of treating waste oil
RU2815U1 (en) * 1994-06-30 1996-09-16 Владимир Леонидович Жеребцов Oil regeneration installation
RU2288946C2 (en) * 2002-07-15 2006-12-10 Сенер Групо Де Инхенерия, С.А. Method of purification of the waste oils using extraction by dissolvents
RU2326934C2 (en) * 2006-06-20 2008-06-20 Государственное образовательное учреждение высшего профессионального образования "Кузбасский государственный технический университет" (ГУ КузГТУ) Method of spent industrial oils regeneration and device for its implementation

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4894140A (en) * 1986-11-12 1990-01-16 Schoen Christian O Method of treating waste oil
DE3738391A1 (en) * 1987-11-12 1989-05-24 Wilhelm Joachim A Dr Ing Process for removing impurities by distillation from used oil
RU2815U1 (en) * 1994-06-30 1996-09-16 Владимир Леонидович Жеребцов Oil regeneration installation
RU2288946C2 (en) * 2002-07-15 2006-12-10 Сенер Групо Де Инхенерия, С.А. Method of purification of the waste oils using extraction by dissolvents
RU2326934C2 (en) * 2006-06-20 2008-06-20 Государственное образовательное учреждение высшего профессионального образования "Кузбасский государственный технический университет" (ГУ КузГТУ) Method of spent industrial oils regeneration and device for its implementation

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2728970C1 (en) * 2020-02-04 2020-08-03 Общество с ограниченной ответственностью "НефтеХимКонсалт" Method of two-stage thermal regeneration of waste industrial fluids

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