CN111589293A - Chlorinated fatty acid methyl ester tail gas non-alkalization treatment system - Google Patents
Chlorinated fatty acid methyl ester tail gas non-alkalization treatment system Download PDFInfo
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- CN111589293A CN111589293A CN202010466204.XA CN202010466204A CN111589293A CN 111589293 A CN111589293 A CN 111589293A CN 202010466204 A CN202010466204 A CN 202010466204A CN 111589293 A CN111589293 A CN 111589293A
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- hydrochloric acid
- tail gas
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- liquid
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- 235000019387 fatty acid methyl ester Nutrition 0.000 title claims abstract description 24
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 145
- 239000002994 raw material Substances 0.000 claims abstract description 17
- -1 unsaturated fatty acid methyl ester Chemical class 0.000 claims abstract description 6
- 239000007791 liquid phase Substances 0.000 claims description 81
- 238000006243 chemical reaction Methods 0.000 claims description 51
- 238000010521 absorption reaction Methods 0.000 claims description 46
- 239000006096 absorbing agent Substances 0.000 claims description 45
- 239000011552 falling film Substances 0.000 claims description 44
- 239000007788 liquid Substances 0.000 claims description 39
- 239000007921 spray Substances 0.000 claims description 38
- 238000000746 purification Methods 0.000 claims description 31
- 239000012071 phase Substances 0.000 claims description 24
- 239000002253 acid Substances 0.000 claims description 18
- 238000000926 separation method Methods 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- WRIDQFICGBMAFQ-UHFFFAOYSA-N (E)-8-Octadecenoic acid Natural products CCCCCCCCCC=CCCCCCCC(O)=O WRIDQFICGBMAFQ-UHFFFAOYSA-N 0.000 claims description 6
- LQJBNNIYVWPHFW-UHFFFAOYSA-N 20:1omega9c fatty acid Natural products CCCCCCCCCCC=CCCCCCCCC(O)=O LQJBNNIYVWPHFW-UHFFFAOYSA-N 0.000 claims description 6
- QSBYPNXLFMSGKH-UHFFFAOYSA-N 9-Heptadecensaeure Natural products CCCCCCCC=CCCCCCCCC(O)=O QSBYPNXLFMSGKH-UHFFFAOYSA-N 0.000 claims description 6
- ZQPPMHVWECSIRJ-UHFFFAOYSA-N Oleic acid Natural products CCCCCCCCC=CCCCCCCCC(O)=O ZQPPMHVWECSIRJ-UHFFFAOYSA-N 0.000 claims description 6
- 239000005642 Oleic acid Substances 0.000 claims description 6
- QXJSBBXBKPUZAA-UHFFFAOYSA-N isooleic acid Natural products CCCCCCCC=CCCCCCCCCC(O)=O QXJSBBXBKPUZAA-UHFFFAOYSA-N 0.000 claims description 6
- ZQPPMHVWECSIRJ-KTKRTIGZSA-N oleic acid Chemical compound CCCCCCCC\C=C/CCCCCCCC(O)=O ZQPPMHVWECSIRJ-KTKRTIGZSA-N 0.000 claims description 6
- 238000003860 storage Methods 0.000 claims description 6
- 230000001502 supplementing effect Effects 0.000 claims description 6
- 239000000945 filler Substances 0.000 claims description 5
- NEHMKBQYUWJMIP-UHFFFAOYSA-N anhydrous methyl chloride Natural products ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 claims 1
- 235000014113 dietary fatty acids Nutrition 0.000 claims 1
- 239000000194 fatty acid Substances 0.000 claims 1
- 229930195729 fatty acid Natural products 0.000 claims 1
- 239000010408 film Substances 0.000 claims 1
- 229940050176 methyl chloride Drugs 0.000 claims 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 abstract description 22
- 239000000460 chlorine Substances 0.000 abstract description 22
- 229910052801 chlorine Inorganic materials 0.000 abstract description 22
- 235000021122 unsaturated fatty acids Nutrition 0.000 abstract description 5
- 239000012535 impurity Substances 0.000 abstract description 4
- 238000006298 dechlorination reaction Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 70
- 239000003921 oil Substances 0.000 description 39
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 9
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 9
- 238000005457 optimization Methods 0.000 description 9
- 238000000034 method Methods 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 3
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 210000003298 dental enamel Anatomy 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000007259 addition reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 239000004014 plasticizer Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/68—Halogens or halogen compounds
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/07—Purification ; Separation
- C01B7/0706—Purification ; Separation of hydrogen chloride
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/202—Single element halogens
- B01D2257/2025—Chlorine
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0001—Separation or purification processing
- C01B2210/0003—Chemical processing
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0001—Separation or purification processing
- C01B2210/0009—Physical processing
- C01B2210/0025—Physical processing by absorption in liquids
Abstract
The invention discloses a chlorinated fatty acid methyl ester tail gas non-alkalization treatment system, and relates to the field of chlorinated fatty acid methyl ester tail gas treatment. The invention adopts a counter-current mode, uses fresh raw oil unsaturated fatty acid methyl ester to react and remove chlorine in the tail gas, fully utilizes the raw material chlorine in the tail gas, greatly improves the dechlorination efficiency, realizes the final alkali-free tail gas treatment, and finally obtains concentrated hydrochloric acid with less impurities and high quality through the system. The invention has potential market value.
Description
Technical Field
The invention relates to the field of chlorinated fatty acid methyl ester tail gas treatment, in particular to a non-alkalization treatment system for chlorinated fatty acid methyl ester tail gas.
Background
Chlorinated fatty acid methyl ester is a novel green environment-friendly plasticizer developed only in recent years and is prepared by reacting unsaturated fatty acid methyl ester with chlorine under certain conditions. During the production process, a large amount of tail gas is generated, and the components of the tail gas mainly comprise hydrogen chloride generated by a large amount of reaction, a small amount of chlorine which does not participate in the reaction due to insufficient reaction and oil gas carried away by airflow in the high-temperature violent reaction process. The general treatment method is that the tail gas is firstly converted into hydrochloric acid by the absorption tower, then the hydrochloric acid is absorbed by the tail gas through the alkali pool, and finally the tail gas is discharged. However, such a treatment has the following disadvantages: (1) the utilization rate of chlorine is low, and the purification equipment is complex; (2) the prepared concentrated hydrochloric acid has poor quality, contains a certain amount of free chlorine, has yellow color and more organic impurities; (3) the tail gas is finally absorbed by alkali liquor, the treatment cost of the formed waste water is high, and the tail gas does not meet the environmental protection requirement.
Disclosure of Invention
In order to solve the technical problem, the invention discloses a chlorinated fatty acid methyl ester tail gas non-alkalization treatment system, which comprises a tail gas pretreatment system, an acid making system and an oleic acid separation system; the tail gas pretreatment system comprises at least two reaction absorption kettles and a first gas-liquid separator which are sequentially connected through a gas-phase pipeline, the first gas-liquid separator is sequentially connected with a gate-closing kettle, a purification tower and two reaction absorption kettles through a liquid-phase pipeline, the gate-closing kettle is further connected with a second gas-liquid separator through the gas-phase pipeline and the liquid-phase pipeline, and the gate-closing kettle is further connected with an external raw material oil source through a raw material oil inlet; the acid making system comprises a first-stage falling film absorber connected with a first gas-liquid separator through a gas-phase pipeline, a second-stage falling film absorber, a first-stage spray tower and a second-stage spray tower which are sequentially connected with a second gas-liquid separator through a gas-phase pipeline, wherein the bottom ends of the first-stage falling film absorber and the second-stage falling film absorber are respectively connected with the top end of a concentrated hydrochloric acid circulating tank through liquid-phase pipelines, the bottom end of the concentrated hydrochloric acid circulating tank is respectively connected with the upper parts of the first-stage falling film absorber and the second-stage falling film absorber through liquid-phase pipelines, the bottom ends of the first-stage spray tower and the second-stage spray tower are respectively connected with the top end of a dilute hydrochloric acid circulating tank through liquid-phase pipelines, and the bottom end of the dilute hydrochloric acid circulating tank is; the oleic acid separation system comprises an oil removal tower and a purification tower, wherein an oil removal tower inlet at the upper end of the oil removal tower is connected with the purification tower through a liquid phase pipeline, and an oil removal tower outlet at the lower end of the oil removal tower enters an acid storage through an acid outlet pipeline to be made into a finished product for storage.
As a further optimization of the technical scheme of the invention, a liquid phase pipeline between the primary falling film absorber and the concentrated hydrochloric acid circulating tank is respectively provided with a first liquid phase branch pipe, and the other end of the first liquid phase branch pipe is connected with the purification tower; and a second liquid phase branch pipe is arranged on a liquid phase pipeline between the first-stage spray tower and the dilute hydrochloric acid circulating tank, and the other end of the second liquid phase branch pipe is connected with the concentrated hydrochloric acid circulating tank.
As a further optimization of the technical scheme of the invention, the gas outlet of the secondary spray tower is connected with an exhaust tower through a gas phase pipeline, and the height of the exhaust tower is more than or equal to 25 m.
As a further optimization of the technical scheme of the invention, the reaction absorption kettle and the closure kettle are respectively provided with an airflow distributor.
As a further optimization of the technical scheme of the invention, the reaction absorption kettle and the closure kettle are respectively filled with fillers.
As a further optimization of the technical scheme of the invention, the temperature of the reaction absorption kettle is 70-110 ℃.
As a further optimization of the technical scheme of the invention, a first valve is arranged at a position, close to the purification tower, of the first liquid phase branch pipe, a second valve is arranged at a position, close to the concentrated hydrochloric acid circulation tank, of a liquid phase pipeline between the primary falling film absorber and the concentrated hydrochloric acid circulation tank, a third valve is arranged at a position, close to the concentrated hydrochloric acid circulation tank, of the second liquid phase branch pipe, and a fourth valve is arranged at a position, close to the dilute hydrochloric acid circulation tank, of a liquid phase pipeline between the primary spray tower and the dilute hydrochloric acid circulation tank.
As a further optimization of the technical scheme of the invention, the dilute hydrochloric acid circulating tank is also externally connected with a water supplementing pipeline, and the other end of the water supplementing pipeline is connected with an external water source.
As a further optimization of the technical scheme of the invention, a liquid phase pipeline at the bottom end of the concentrated hydrochloric acid circulating tank is sequentially connected with a first power device and a first liquid path distributor, and the first liquid path distributor is respectively connected with the primary falling film absorber and the secondary falling film absorber through two liquid phase pipelines; and the liquid phase pipeline at the bottom of the dilute hydrochloric acid circulating tank is sequentially connected with a second power device and a second liquid phase distributor, and the second liquid phase distributor is respectively connected with the first-stage spray tower and the second-stage spray tower through two liquid phase pipelines.
As a further optimization of the technical scheme of the invention, a liquid phase pipeline connecting an oil removal tower inlet at the upper end of the oil removal tower and the purification tower is provided with a third liquid phase branch pipe, and the third liquid phase branch pipe is an inverted U-shaped pipeline.
The invention has the beneficial effects that:
(1) no alkalization absorption tail gas: after the tail gas is absorbed by the first-stage falling film absorber, most hydrogen chloride gas is converted into hydrochloric acid, so that the chlorine ratio of the residual tail gas is increased, and the overall gas velocity is reduced. The higher ratio of chlorine can promote the reaction efficiency, and the lower integral gas speed can increase the contact time between the gas and the raw oil. And because the preparation of the chlorinated fatty acid methyl ester is different from the preparation of chlorinated paraffin, the raw material of the chlorinated fatty acid methyl ester contains a large amount of unsaturated double bonds, and chlorine gas is not dissolved firstly but is subjected to addition reaction quickly after being introduced, so that the residual chlorine can be ensured to be completely reacted. In a word, the arrangement of the closing kettle greatly improves the dechlorination efficiency and realizes the final treatment of the tail gas without alkalization.
(2) Preparing high-quality concentrated hydrochloric acid: compared with other related processes, namely 'one-step purification extraction', the system is designed to separate the oil removal tower from the purification tower during the purification of the crude concentrated hydrochloric acid, so that although equipment is added, the efficiency is improved, and the separation effect is better. Wherein, the crude concentrated hydrochloric acid in the purification tower can be quickly extracted and heat-exchanged with the raw oil and then enters the chlorination reaction kettle, thereby greatly saving energy. Meanwhile, the purification tower can purify the organic oil phase impurities in the crude concentrated hydrochloric acid and further absorb the free chlorine possibly existing in the crude concentrated hydrochloric acid, thereby further playing a 'gate keeping role'. In addition, the oil removal tower can utilize a large-volume and high tank body to separate oil and acid in sufficient time and space, and concentrated hydrochloric acid finally obtained through the design has few impurities and high quality.
(3) Energy conservation: the reaction absorption kettle, the closing kettle and the purification tower not only absorb residual chlorine by using raw oil, but also exchange heat between cold oil, hot gas and hot acid and then enter the main reaction kettle, thereby saving energy.
Drawings
In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the drawings needed to be used in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained according to these drawings without inventive labor.
Fig. 1 is a schematic structural diagram in a first embodiment of the present invention.
Fig. 2 is a schematic structural diagram in the second embodiment of the present invention.
Reference numerals:
in fig. 1 and fig. 2, B1 is a first reaction absorption kettle, B2 is a second reaction absorption kettle, B3 is a second control kettle, B4 is a third reaction absorption kettle, M1 is a first gas-liquid separator, M2 is a second gas-liquid separator, E1 is a first-stage falling film absorber, E2 is a second-stage falling film absorber, E3 is a first-stage spray tower, E4 is a second-stage spray tower, E4 is an exhaust tower, C4 is a concentrated hydrochloric acid circulation tank, C4 is a dilute hydrochloric acid circulation tank, C4 is an oil removal tower, C4 is a purification tower, a4 is a gas flow distributor, L4 is a first liquid phase branch pipe, L4 is a third branch pipe, V4 is a first valve, V4 is a second valve, V4 is a third valve, V4 is a fourth valve, T4 is a first power plant, T4 is a second power plant, T4 is a first liquid flow distributor, and D4 is a second liquid flow distributor.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments.
It should be noted that all the directional indicators (such as up, down, left, right, front, and rear … …) in the embodiment of the present invention are only used to explain the relative position relationship between the components, the movement situation, etc. in a specific posture (as shown in the drawing), and if the specific posture is changed, the directional indicator is changed accordingly.
In the description of the embodiments, the terms "disposed," "connected," and the like are to be construed broadly unless otherwise explicitly specified or limited. For example, the connection can be fixed, detachable or integrated; can be mechanically or electrically connected; either directly or through an intervening medium, or through internal communication between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In addition, the descriptions related to "first", "second", etc. in the present invention are for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature.
The first embodiment is as follows:
as shown in figure 1, the invention discloses a chlorinated fatty acid methyl ester tail gas non-alkalization treatment system, which comprises a tail gas pretreatment system, an acid making system and an oleic acid separation system; the tail gas pretreatment system comprises a first reaction absorption kettle B1, a second reaction absorption kettle B2 and a first gas-liquid separator M1 which are sequentially connected through a gas-phase pipeline, the first gas-liquid separator M1 is sequentially connected with a second closing kettle B3, a purification tower C4, a second reaction absorption kettle B2 and a first reaction absorption kettle B1 through a liquid-phase pipeline, the second closing kettle B3 is also connected with a second gas-liquid separator M2 through a gas-phase pipeline and a liquid-phase pipeline, and the second closing kettle B3 is also connected with an external raw material oil source through a raw material oil inlet; in the tail gas treatment process, tail gas firstly passes through a tail gas pretreatment system, the tail gas firstly enters a reaction absorption kettle B1 and a reaction absorption kettle II B2 which are connected in series continuously, raw material chlorine which is not utilized in the tail gas reacts with raw material oil unsaturated fatty acid methyl ester which enters from a banister B3 to generate chlorinated fatty acid methyl ester, the generated chlorinated fatty acid methyl ester finally flows out of a production device through a reaction absorption kettle I B1 to be further reacted, the unabsorbed tail gas enters a gas-liquid separator I M1 connected with the reaction absorption kettle B2 through the upper end, a gas phase after gas-liquid separation enters a first-stage falling film absorber E1 in a subsequent acid making system, a liquid phase after gas-liquid separation enters a banister B3, dechlorinated tail gas which is generated by a banister B3 enters a gas-liquid separator II M2 through the upper end, the gas phase after secondary separation enters a second-stage falling film absorber E2 connected with the upper end of a gas-liquid separator II M2, the liquid phase after the secondary separation enters a hold-off kettle B3 again, and chlorine in the tail gas is basically removed through the pretreatment step.
The acid making system comprises a primary falling film absorber E1 connected with a first gas-liquid separator M1 through a gas phase pipeline, a secondary falling film absorber E2 sequentially connected with a second gas-liquid separator M2 through a gas phase pipeline, a primary spray tower E3 and a secondary spray tower E4, wherein the primary falling film absorber E1 and the bottom end of the secondary falling film absorber E2 are respectively connected with the top end of a concentrated hydrochloric acid circulating tank C1 through liquid phase pipelines, the bottom end of the concentrated hydrochloric acid circulating tank C1 is respectively connected with the upper parts of the primary falling film absorber E1 and the secondary falling film absorber E2 through liquid phase pipelines, the bottom ends of the primary spray tower E3 and the secondary spray tower E4 are respectively connected with the top end of a dilute hydrochloric acid circulating tank C2 through liquid phase pipelines, and the bottom end of the dilute hydrochloric acid circulating tank C2 is respectively connected with the primary spray tower E3 and the secondary spray tower E4 through liquid; the gas outlet of the secondary spray tower E4 is connected with an exhaust tower E5 through a gas phase pipeline, and the height of the exhaust tower E5 is more than or equal to 25 m.
Wherein a liquid phase pipeline between the primary falling film absorber E1 and the concentrated hydrochloric acid circulating tank C1 is provided with a first liquid phase branch pipe L1, and the other end of the first liquid phase branch pipe L1 is connected with a purification tower C4; a liquid phase pipeline between the first-stage spray tower E3 and the dilute hydrochloric acid circulating tank C2 is provided with a second liquid phase branch pipe L2, the other end of the second liquid phase branch pipe L2 is connected with a concentrated hydrochloric acid circulating tank C1, a first valve V1 is arranged at a position, close to the purifying tower C4, of the first liquid phase branch pipe L1, a second valve V2 is arranged at a position, close to the concentrated hydrochloric acid circulating tank C1, of the liquid phase pipeline between the first-stage falling film absorber E1 and the concentrated hydrochloric acid circulating tank C1, a third valve V3 is arranged at a position, close to the concentrated hydrochloric acid circulating tank C1, of the second liquid phase branch pipe L2, and a fourth valve V4 is arranged at a position, close to the dilute hydrochloric acid circulating tank C2, of the liquid phase pipeline between the first-stage.
The concentrated hydrochloric acid circulating tank C1 and the dilute hydrochloric acid circulating tank C2 are provided with hydrochloric acid concentration sensors, the hydrochloric acid concentration sensors are connected with an external control device, the external control device is connected with valves V1, V2, V3 and V4, so that the purpose of controlling the opening and closing of the valves according to the hydrochloric acid concentration is achieved, and the external control device can select a PLC (programmable logic controller) and the like.
The tail gas is primarily cleared of chlorine in a first reaction absorption kettle B1 and a second reaction absorption kettle B2 and then enters an acid making system, the tail gas contains a large amount of HCl gas, the HCl gas enters a first-stage falling film absorber E1 from a first gas-liquid separator M1, and the HCl gas is mostly cleared away by concentrated hydrochloric acid generated by the tail gas and moisture in the first-stage falling film absorber E1, at the moment, the concentration of chlorine in the tail gas is increased, the tail gas enters a gate keeping kettle B3 from the first-stage falling film absorber E1, and the chlorine gas is more easily cleared in a gate keeping kettle B3. After the tail gas comes out from the gate-holding kettle B3, the tail gas enters a gas-liquid separator II M2 for further separation, the separated liquid phase returns to the gate-holding kettle B3 again, the separated gas phase enters a secondary falling film absorber E2, a primary falling film absorber E1, a secondary falling film absorber E2 and a concentrated hydrochloric acid circulating tank C1 form internal circulation, HCl gas in the tail gas is continuously absorbed, when the concentrated hydrochloric acid is higher than the set concentration, a first valve V1 is opened, a second valve V2 is closed, the concentrated hydrochloric acid enters a purification tower C4 for oil removal and free chlorine removal purification, when the concentrated hydrochloric acid is lower than the set concentration, the first valve V1 is closed, the second valve V2 is opened, and the concentrated hydrochloric acid continues to circulate and enrich.
After chlorine and most of HCl gas are removed from tail gas, the tail gas sequentially enters a first-stage spray tower E3 and a second-stage spray tower E4 from a second-stage falling film absorber E2 to contact with moisture in the tail gas to continuously remove the residual HCl gas, internal circulation is formed among the first-stage spray tower E3, the second-stage spray tower E4 and a dilute hydrochloric acid circulating tank C2 to continuously absorb the entering residual HCl gas, when the dilute hydrochloric acid is higher than a set concentration, a third valve V3 is opened, a fourth valve V4 is closed, the dilute hydrochloric acid enters a concentrated hydrochloric acid circulating tank C1 to supplement the concentrated hydrochloric acid circulating tank so as to finally enter a purification tower C4 to remove oil and free chlorine for purification, and when the dilute hydrochloric acid is lower than the set concentration, the third valve V3 is closed, the fourth valve V4 is opened, and the dilute hydrochloric acid is continuously circulated and concentrated.
The oleic acid separation system comprises an oil removal tower C3 and a purification tower C4, wherein an oil removal tower inlet at the upper end of the oil removal tower C3 is connected with the purification tower C4 through a liquid phase pipeline, after the acid preparation step is completed, concentrated hydrochloric acid in the purification tower C4 and an oil phase from a banister kettle B3 are further extracted and washed, a small amount of chlorine and the oil phase carried in the concentrated hydrochloric acid are removed, the concentrated hydrochloric acid is further purified, finally enters the oil removal tower C3, and the oil phase is finally separated and then enters an acid storage to be prepared into products for storage. An oil removal tower inlet purification tower C4 at the upper end of an oil removal tower C3 is connected with a liquid phase pipeline and is provided with a third liquid phase branch pipe L3, the third liquid phase branch pipe L3 is an inverted U-shaped pipeline, the inverted U-shaped pipeline is arranged by utilizing the characteristics of acid oil layering and light acid heavy oil, hydrochloric acid is continuously discharged from a bottom liquid phase pipeline, accumulated oil reaches a certain liquid level and is automatically recycled after backflow, and finally, the complete de-oiling of byproduct hydrochloric acid can be realized.
Preferably, a liquid phase pipeline at the bottom end of the concentrated hydrochloric acid circulation tank C1 is sequentially connected with a first power device T1 and a first liquid path distributor D1, and the first liquid path distributor D1 is respectively connected with the primary falling film absorber E1 and the secondary falling film absorber E2 through two liquid phase pipelines, so that internal circulation is formed among the primary falling film absorber E1, the secondary falling film absorber E2 and the concentrated hydrochloric acid circulation tank C1; the liquid phase pipeline at the bottom of the dilute hydrochloric acid circulating tank C2 is sequentially connected with a second power T2 device and a second liquid phase distributor D2, and the second liquid phase distributor D2 is respectively connected with a first-stage spray tower and a second-stage spray tower E4 of the E3 through two liquid phase pipelines, so that internal circulation is formed among the first-stage spray tower E3, the second-stage spray tower E4 and the dilute hydrochloric acid circulating tank C2. The dilute hydrochloric acid circulating tank C1 is also externally connected with a water supplementing pipeline, and the other end of the water supplementing pipeline is connected with an external water source, so that the water can be used by the first-stage spray tower E3 and the second-stage spray tower E4.
Wherein, the first reaction absorption kettle B1, the second reaction absorption kettle B2 and the second bang kettle B3 are respectively provided with an air flow distributor A1/A2 and an air flow distributor A3 or are respectively filled with fillers, so that the air and the liquid in each kettle can be fully contacted, and the fillers can be enamel fillers such as pall rings, enamel rings, Raschi rings and the like.
Wherein the temperature in the first reaction absorption kettle B1 and the second reaction absorption kettle B2 is 70-110 ℃, and the unused raw material chlorine in the tail gas can fully react with the raw material oil unsaturated fatty acid methyl ester entering from the Baker kettle B3 in the temperature range.
The reaction absorption kettles are not limited to the first reaction absorption kettle B1 and the second reaction absorption kettle B2, and a plurality of reaction absorption kettles can be arranged according to the process requirement.
Example two:
when three reaction absorption kettles are arranged, as shown in fig. 2, the tail gas pretreatment system comprises a first reaction absorption kettle B1, a second reaction absorption kettle B2, a third reaction absorption kettle B4 and a first gas-liquid separator M1 which are sequentially connected through a gas phase pipeline, the first gas-liquid separator M1 is sequentially connected with a second closing kettle B3, a purification tower C4, a third reaction absorption kettle B4, a second reaction absorption kettle B2 and a first reaction absorption kettle B1 through a liquid phase pipeline, the second closing kettle B3 is also connected with a second gas-liquid separator M2 through a gas phase pipeline and a liquid phase pipeline, and the second closing kettle B3 is also connected with an external raw material oil source through a raw material oil inlet; in the tail gas treatment process, tail gas sequentially enters a first reaction absorption kettle B1, a second reaction absorption kettle B2, a third reaction absorption kettle B4 and a first-stage falling film absorber E1, and finally enters a first closing kettle B3, raw material chlorine which is not utilized in the tail gas reacts with raw material oil unsaturated fatty acid methyl ester entering from the first closing kettle B3 in the four kettles to generate chlorinated fatty acid methyl ester, and the generated chlorinated fatty acid methyl ester finally flows out of the first reaction absorption kettle B1 to a production device for further reaction. Under the same working conditions, the unused raw material chlorine in the tail gas reacts more fully. The rest parts and the working principle are the same as the above parts, and the detailed description is omitted here.
In actual production, the number of required reaction absorption kettles can be determined by comprehensively considering equipment cost and process requirements.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein. In addition, the technical solutions between the various embodiments can be combined with each other, but must be based on the realization of those skilled in the art; where combinations of features are mutually inconsistent or impractical, such combinations should not be considered as being absent and not within the scope of the claimed invention.
Claims (10)
1. The non-alkalization treatment system for the tail gas of the methyl chloride fatty acid is characterized in that: comprises a tail gas pretreatment system, an acid making system and an oleic acid separation system;
the tail gas pretreatment system comprises at least two reaction absorption kettles and a first gas-liquid separator which are sequentially connected through a gas-phase pipeline, the first gas-liquid separator is sequentially connected with a gate-closing kettle, a purification tower and two reaction absorption kettles through a liquid-phase pipeline, the gate-closing kettle is further connected with a second gas-liquid separator through the gas-phase pipeline and the liquid-phase pipeline, and the gate-closing kettle is further connected with an external raw material oil source through a raw material oil inlet;
the acid making system comprises a first-stage falling film absorber connected with a first gas-liquid separator through a gas-phase pipeline, a second-stage falling film absorber, a first-stage spray tower and a second-stage spray tower which are sequentially connected with a second gas-liquid separator through a gas-phase pipeline, wherein the bottom ends of the first-stage falling film absorber and the second-stage falling film absorber are respectively connected with the top end of a concentrated hydrochloric acid circulating tank through liquid-phase pipelines, the bottom end of the concentrated hydrochloric acid circulating tank is respectively connected with the upper parts of the first-stage falling film absorber and the second-stage falling film absorber through liquid-phase pipelines, the bottom ends of the first-stage spray tower and the second-stage spray tower are respectively connected with the top end of a dilute hydrochloric acid circulating tank through liquid-phase pipelines, and the bottom end of the dilute hydrochloric acid circulating tank is;
the oleic acid separation system comprises an oil removal tower and a purification tower, wherein an oil removal tower inlet at the upper end of the oil removal tower is connected with the purification tower through a liquid phase pipeline, and an oil removal tower outlet at the lower end of the oil removal tower enters an acid storage through an acid outlet pipeline to be made into a finished product for storage.
2. The non-alkalization treatment system for chlorinated fatty acid methyl ester tail gas according to claim 1, characterized in that: a liquid phase pipeline between the primary falling film absorber and the concentrated hydrochloric acid circulating tank is provided with a first liquid phase branch pipe, and the other end of the first liquid phase branch pipe is connected with the purification tower; and a second liquid phase branch pipe is arranged on a liquid phase pipeline between the first-stage spray tower and the dilute hydrochloric acid circulating tank, and the other end of the second liquid phase branch pipe is connected with the concentrated hydrochloric acid circulating tank.
3. The non-alkalization treatment system for chlorinated fatty acid methyl ester tail gas according to claim 1, characterized in that: and the gas outlet of the secondary spray tower is connected with an exhaust tower through a gas phase pipeline, and the height of the exhaust tower is more than or equal to 25 m.
4. The non-alkalization treatment system for chlorinated fatty acid methyl ester tail gas according to claim 1, characterized in that: and the reaction absorption kettle and the handle kettle are respectively provided with an airflow distributor.
5. The non-alkalization treatment system for chlorinated fatty acid methyl ester tail gas according to claim 1, characterized in that: and the reaction absorption kettle and the closure kettle are respectively filled with fillers.
6. The non-alkalization treatment system for chlorinated fatty acid methyl ester tail gas according to claim 1, characterized in that: the temperature of the reaction absorption kettle is 70-110 ℃.
7. The non-alkalization treatment system for chlorinated fatty acid methyl ester tail gas according to claim 2, characterized in that: first liquid phase branch pipe is close to purification tower department is provided with first valve, one-level falling liquid film absorber with liquid phase pipeline between the concentrated hydrochloric acid circulation jar is close to concentrated hydrochloric acid circulation jar department is provided with the second valve, second liquid phase branch pipe is close to concentrated hydrochloric acid circulation jar department is provided with the third valve, one-level spray column with liquid phase pipeline between the dilute hydrochloric acid circulation jar is close to dilute hydrochloric acid circulation jar department is provided with the fourth valve.
8. The non-alkalization treatment system for chlorinated fatty acid methyl ester tail gas according to claim 1, characterized in that: the dilute hydrochloric acid circulating tank is also externally connected with a water supplementing pipeline, and the other end of the water supplementing pipeline is connected with an external water source.
9. The non-alkalization treatment system for chlorinated fatty acid methyl ester tail gas according to claim 1, characterized in that: a liquid phase pipeline at the bottom end of the concentrated hydrochloric acid circulating tank is sequentially connected with a first power device and a first liquid path distributor, and the first liquid path distributor is respectively connected with the primary falling film absorber and the secondary falling film absorber through two liquid phase pipelines; and the liquid phase pipeline at the bottom of the dilute hydrochloric acid circulating tank is sequentially connected with a second power device and a second liquid phase distributor, and the second liquid phase distributor is respectively connected with the first-stage spray tower and the second-stage spray tower through two liquid phase pipelines.
10. The non-alkalization treatment system for chlorinated fatty acid methyl ester tail gas according to claim 1, characterized in that: an oil removing tower inlet at the upper end of the oil removing tower is connected with the purification tower through a liquid phase pipeline, and a third liquid phase branch pipe is an inverted U-shaped pipeline.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115634642A (en) * | 2021-07-19 | 2023-01-24 | 河北大景大搪化工设备有限公司 | Chlorinated fatty acid methyl ester reaction tower and preparation device formed by same |
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| CN104560197A (en) * | 2014-12-23 | 2015-04-29 | 丹阳市助剂化工厂有限公司 | Tail gas processing process of chlorinated paraffin |
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Address after: 264000 North 50 meters east of the intersection of Liaoning Road and Zhejiang Road, Economic Development Zone, Fushan District, Yantai City, Shandong Province Applicant after: Shandong Zhenxi New Material Technology Co.,Ltd. Address before: 264000 North shouyixin e-commerce Industrial Park, Xianxia Road, Qixia City, Yantai City, Shandong Province Applicant before: Shandong Zhenxi New Material Technology Co.,Ltd. |
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Application publication date: 20200828 |