CN106010649A - Chlorinated paraffin continuous production process efficiently utilizing chlorine gas - Google Patents
Chlorinated paraffin continuous production process efficiently utilizing chlorine gas Download PDFInfo
- Publication number
- CN106010649A CN106010649A CN201610626069.4A CN201610626069A CN106010649A CN 106010649 A CN106010649 A CN 106010649A CN 201610626069 A CN201610626069 A CN 201610626069A CN 106010649 A CN106010649 A CN 106010649A
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- Prior art keywords
- reactor
- chlorine
- tail gas
- reaction kettle
- chlorinated paraffin
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- 239000012188 paraffin wax Substances 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims abstract description 29
- 230000008569 process Effects 0.000 title claims abstract description 14
- 238000010924 continuous production Methods 0.000 title claims abstract description 10
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 title abstract 7
- 238000006243 chemical reaction Methods 0.000 claims abstract description 49
- 239000000047 product Substances 0.000 claims abstract description 20
- 239000005662 Paraffin oil Substances 0.000 claims abstract description 18
- 230000000694 effects Effects 0.000 claims abstract description 8
- 239000006227 byproduct Substances 0.000 claims abstract description 6
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 76
- 239000000460 chlorine Substances 0.000 claims description 73
- 229910052801 chlorine Inorganic materials 0.000 claims description 73
- 239000007789 gas Substances 0.000 claims description 39
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 24
- 238000001514 detection method Methods 0.000 claims description 15
- 238000005660 chlorination reaction Methods 0.000 claims description 14
- 238000001816 cooling Methods 0.000 claims description 13
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims description 13
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims description 12
- 238000004519 manufacturing process Methods 0.000 claims description 11
- 238000010521 absorption reaction Methods 0.000 claims description 9
- 239000003513 alkali Substances 0.000 claims description 5
- 238000005516 engineering process Methods 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 5
- 239000006096 absorbing agent Substances 0.000 claims description 4
- 230000005540 biological transmission Effects 0.000 claims description 3
- 238000007664 blowing Methods 0.000 claims description 3
- 238000006555 catalytic reaction Methods 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims description 3
- 230000008859 change Effects 0.000 claims description 2
- 239000001257 hydrogen Substances 0.000 claims description 2
- 229910052739 hydrogen Inorganic materials 0.000 claims description 2
- -1 reactor group Chemical compound 0.000 claims description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims 1
- 238000011084 recovery Methods 0.000 abstract 1
- 230000004044 response Effects 0.000 description 5
- 230000001276 controlling effect Effects 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 230000003247 decreasing effect Effects 0.000 description 2
- 239000003063 flame retardant Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 230000001699 photocatalysis Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000001993 wax Substances 0.000 description 2
- 125000006414 CCl Chemical group ClC* 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 206010054949 Metaplasia Diseases 0.000 description 1
- 239000005708 Sodium hypochlorite Substances 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 238000010923 batch production Methods 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000004992 fission Effects 0.000 description 1
- 239000003292 glue Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000002649 leather substitute Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 230000015689 metaplastic ossification Effects 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000004014 plasticizer Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G73/00—Recovery or refining of mineral waxes, e.g. montan wax
- C10G73/38—Chemical modification of petroleum
-
- 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
- B01D53/14—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 by absorption
- B01D53/1406—Multiple stage absorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
- B01J19/12—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electromagnetic waves
- B01J19/122—Incoherent waves
- B01J19/123—Ultraviolet light
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/245—Stationary reactors without moving elements inside placed in series
-
- 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
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00162—Controlling or regulating processes controlling the pressure
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
- Toxicology (AREA)
- Health & Medical Sciences (AREA)
- Analytical Chemistry (AREA)
- Electromagnetism (AREA)
- Physics & Mathematics (AREA)
- Inorganic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a chlorinated paraffin continuous production process efficiently utilizing chlorine gas. The process involves a reaction kettle group. The reaction kettle group comprises a first reaction kettle, a second reaction kettle, a third reaction kettle, a fourth reaction kettle, a fifth reaction kettle and a sixth reaction kettle, each reaction kettle is internally equipped with an ultraviolet lamp, paraffin oil enters the first reaction kettle continuously, chlorine gas enters the chlorine gas inlet of each reaction kettle from a chlorine gas supply main pipe, the product of previous stage reaction enters a next stage reaction kettle, and the tail gas obtained in the sixth reaction kettle is collected overall and then enters a tail gas main pipe, and is introduced into a tail gas main pipe system to produce by-products. Through secondary utilization of tail gas, chlorine gas in the tail gas can fully react, thus providing the chlorine gas utilization and achieving the energy saving and emission reduction effects. The tail gas component is single, thereby being convenient for recovery and utilization of tail gas.
Description
Technical field
The present invention relates to a kind of chlorinated-paraffin producing process, in particular, relate to a kind of chlorination stone that can efficiently utilize chlorine
Wax production technology.
Background technology
Chlorinated paraffin has that volatility is low, fire-retardant, electrical insulating property is good and many excellent physicochemical properties such as resistance to chemical attack, available
Make fire retardant polrvinyl chloride secondary plasticizer(-iser) etc., be widely used in produce plastics, cable, plate, flexible pipe, artificial leather and rubber
Glue goods etc. are it can also be used to the additive of paint, coating and lubricating oil etc..Due to chlorinated paraffin importance in commercial Application,
Therefore the optimization of its production method, arouses widespread concern.
At present, the mode of production of chlorinated paraffin mainly has thermal chlorination and photocatalytic method.
The thermal chlorination response time is long, and the response time such as chlorinated paraffin-52 is typically for up to about 60h, cause production efficiency low,
The phenomenons such as energy consumption height is low with chlorine utilization highlight.
Photocatalytic method is to promote chlorine molecule covalent bond fission to be dissociated into chlorine radical with the ultraviolet light of about 340nm, the state of activation
Chlorine radical bombards paraffin molecule continuously and forms C-Cl key, accelerates reaction rate, and the response time generating paraffin-52 is down to
24-36h (and 24-38h).But, the theoretical and practical production experience according to bimodulus, the course of reaction of chlorinated paraffin is homogeneous reaction,
Chlorine is first dissolved in paraffin the most just chemical reaction, and chlorine dissolution velocity in paraffin is less than response speed, the most whole
Reaction is mass transport limitation step
In three of the above mode, it is the most extensive that the third uses that the mode of light chlorination process applies, in order to use seriality and big
The production of scale, can use multiple reactor and be used in series in prior art, " company as entitled in Patent No. 200610025410.7
Continuous metaplasia produces the method for chlorinated paraffin " Chinese patent in, just used this mode, then continuous regardless of mode
Property produce chlorinated paraffin method in, each reactor all can produce tail gas, and tail gas is chlorine and hydrogen chloride, existing side
In method, it is directly the tail gas produced in each reactor to be collected, enters in exhaust treatment system, this mode, will
The supply making chlorine becomes huge, the most well utilizes for chlorine present in tail gas, increases production cost.
Summary of the invention
The deficiency existed for prior art, it is an object of the invention to provide a kind of chlorinated paraffin efficiently utilizing chlorine and gives birth to continuously
Production. art, it is possible to make the utilization rate of the chlorine in the tail gas in each reactor obtain maximized secondary and utilize.
For achieving the above object, the technical scheme is that
A kind of chlorinated paraffin continuous production processes efficiently utilizing chlorine, including reactor group, this reactor group includes the first reaction
Still, to the 6th reactor, is fitted with uviol lamp in each reactor, and each reactor is equipped with material cooling system, and this is cold
But system includes out cooling down circulating line from the bottom of each reactor, responds product in this cooling circulating line, and this is anti-
Answer product to enter the entrance of cooler, be cooled to 83-88 degree, then by the effect of circulating pump from the top respective reaction of entrance
Still；Reaction temperature controls to be 95-100 degree, and reaction pressure is 0.02-0.03Mpa；
Each reactor is equipped with respective pressure detecting and controls flow-route and temperature detection control technique, and pressure detecting controls technique；
Manual detection densimeter and electronic long-distance transmission densimeter are installed on the 4th reactor and the 6th reactor；
This production technology includes: paraffin oil enters the first reactor by paraffin oil entrance continuous print, and chlorine is from chlorine supply main
Respectively enteing in the chlorine inlet of each reactor, paraffin oil in the first reactor and chlorine, under the catalysis of ultraviolet light, enter
Row chlorination, and entered in the reactor of next stage by the upper level chlorination oil that obtains of reaction and paraffin oil mixture, even
Continuous reaction, the product that the 6th reactor obtains enters in chlorinated paraffin medial launder and collects；The hydrogen chloride of reaction generation and centre
The chlorine the being mingled with offgas outlet from the top of the reactor of previous stage enters into next stage reactor, and last 6th anti-
The tail gas answering still to obtain carries out general collection and enters engine manifold, is passed through exhaust treatment system and generates side-product；First reactor is extremely
A diameter of 4th reactor of the chlorine inlet pipeline of the 3rd reactor to the chlorine inlet pipeline of the 6th reactor diameter two
Times, corresponding chlorine supply flow control four reactor is to the half that the 6th reactor is the first reactor to the 3rd reactor.
By using technique scheme, traditional batch production method change continuous production method into；At each reactor
Middle installation uviol lamp, excites chlorine molecule so that it is be dissociated into chlorine radical so that it carries out sufficient chlorination with paraffin oil；
Maximum changes into, the different from the past mode that the tail gas in each reactor is passed directly to exhaust collection house steward, due to
Tail gas in each reactor can exist and not react sufficient chlorine, thus the mode of this collection tail gas makes chlorine
The utilization rate of gas reduces, and increases raw-material consumption, and here, the tail gas by the reactor generation of upper level is passed into next
In order reaction still, the chlorine of remaining before is entered in the reactor of next stage and carry out secondary response, in the utilization increasing chlorine
While rate, decrease again the supply of original chlorine, reach the effect of energy-saving and emission-reduction；And from the beginning of the 4th reactor,
The half of a diameter of above diameter of the chlorine inlet pipeline of three reactors of chlorine inlet pipeline, thus significantly control chlorine
Trying one's best of gas, the another one effect for amount minimizing at chlorine is the reaction of convenient control chlorinated paraffin so that below
The generation concentration of the chlorinated paraffin in several reactors is more prone to control, and generates chlorinated paraffin by multiple reactor gradual reactions
Mode so that from last reactor, the concentration controlling of the i.e. the 6th reactor chlorinated paraffin out is greatly enhanced, by
Few in the chlorine input of the 6th reactor, the internal chlorine reaction of reactor is more abundant, and from the tail gas that the 6th reactor is discharged,
It is practically free of chlorine, the almost hydrogen chloride gas of discharge, the utilization rate of chlorine is nearly reached the efficiency of 100%, has improved
The supply of total chlorine is decreased again, it is achieved that the effect of energy-conserving and environment-protective while the utilization rate of chlorine, and the composition of tail gas
More single, thus it is more prone to the recycling of tail gas, it is made that, for energy-saving and emission-reduction and high efficiente callback, the breakthrough that matter is general.
In each reactor, it is provided with material cooling system, and controls flow-route and temperature by the pressure detecting of relative set
Detection controls technique, facilitates operator to the observation of each reactor inner case and control, provides for final end product quality
Ensure；By Density Detection technique, owing to the chlorine feed in first three reactor is big, reaction acutely, is not easy in detection
The density of portion's chlorinated paraffin, carries out the most preliminary chlorinated paraffin detection in the 4th reactor, regulates and controls from the data recorded
The charging situation of paraffin oil and chlorine, then carry out secondary accurate detection to the 6th last reactor, it is ensured that final chlorination
The finished product concentration of paraffin, it is ensured that product quality.
The present invention is further arranged to: the 6th reactor is the refined, by the fortune of switching value Valve controlling batch turning pump of chlorinated paraffin
Turn the time, and start blowing still blowout hydrogen chloride feeding exhaust treatment system, release chlorinated paraffin from the bottom of the 6th reactor
Finished product, sends into chlorinated paraffin medial launder.
The present invention is further arranged to: exhaust treatment system the 6th reactor tail gas out is sequentially sent to hydrogen chloride absorption tower,
Two-stage spray column, tail gas absorber and Alkali absorption tower, finally give byproduct hydrochloric acid.
Compared with prior art, it is an advantage of the current invention that:
1, the recycling mode of tail gas is changed so that the chlorine in tail gas is fully used, so that total chlorine obtains
The almost utilization rate of 100%.
2, being capable of the continuous reaction process of chlorinated paraffin, the chlorination reaction time shortens, can by 25-28 hour of traditional handicraft,
Shorten to 20-23 hour.
3, the steady quality of product, energy-saving and emission-reduction.
4, the composition of tail gas is single, it is simple to vent gas treatment, reduces and pollutes.
Accompanying drawing explanation
Fig. 1 is the process chart of chlorinated paraffin continuous production processes embodiment of the present invention
In figure, 11, pressure transmitter；12, temperature transmitter；2, circulating pump；3, cooler.
Detailed description of the invention
1 pair of a kind of chlorinated paraffin continuous production processes embodiment efficiently utilizing chlorine of the present invention is described further referring to the drawings.
The present embodiment includes reactor group, and this reactor group includes the first reactor to the 6th reactor, pacifies in each reactor
Equipped with uviol lamp, each reactor is equipped with material cooling system, and this cooling system includes that the bottom from each reactor goes out
Cooling down circulating line, respond product in this cooling circulating line, this product enters the entrance of cooler, is cooled to 83-88
Degree, then by the effect of circulating pump from the respective reactor of top entrance；Reaction temperature controls as 95-100 degree, reaction pressure
For 0.02-0.03Mpa；
Each reactor is equipped with respective pressure detecting and controls flow-route and temperature detection control technique, and pressure detecting controls technique；
Valve is regulated, it is ensured that the pressure of each reactor is including the pressure transmitter 11 being located on each reactor and chlorine
0.02-0.03Mp。
Manual detection densimeter and electronic long-distance transmission densimeter are installed on the 4th reactor and the 6th reactor；By Density Detection work
Skill, owing to the chlorine feed in first three reactor is big, reaction acutely, is not easy to detect the density of internal chlorinated paraffin,
4th reactor carries out the most preliminary chlorinated paraffin detection, from the data recorded to regulate and control the charging feelings of paraffin oil and chlorine
Condition, then carry out secondary accurate detection to the 6th last reactor, it is ensured that the finished product concentration of final chlorinated paraffin, it is ensured that
Product quality.
This production technology includes: paraffin oil enters the first reactor by paraffin oil entrance continuous print, and chlorine is from chlorine supply main
Respectively enteing in the chlorine inlet of each reactor, paraffin oil in the first reactor and chlorine, under the catalysis of ultraviolet light, enter
Row chlorination, and entered in the reactor of next stage by the upper level chlorination oil that obtains of reaction and paraffin oil mixture, even
Continuous reaction, the product that the 6th reactor obtains enters in chlorinated paraffin medial launder and collects；The hydrogen chloride of reaction generation and centre
The chlorine the being mingled with offgas outlet from the top of the reactor of previous stage enters into next stage reactor, and last 6th anti-
The tail gas answering still to obtain carries out general collection and enters engine manifold, is passed through exhaust treatment system and generates side-product；First reactor is extremely
A diameter of 4th reactor of the chlorine inlet pipeline of the 3rd reactor to the chlorine inlet pipeline of the 6th reactor diameter two
Times, corresponding chlorine supply flow control four reactor is to the half that the 6th reactor is the first reactor to the 3rd reactor.
According to said structure and accompanying drawing, when driving, first open wax feeds pipe, after the liquid level of the first reactor is added to half,
It is passed through chlorine to react, when reaction temperature reaches 83 degree, the product of the first reactor is passed through cooling recirculation system,
The temperature entering the material of cooler 3 is controlled at 83-88 degree, and the temperature in the first reactor controls at 95-100 degree,
Additionally simultaneously, being inputted by reaction mass in the second reactor, the paraffin oil in reactant will continue and is passed through in the second reactor
Chlorine reacts, and simultaneously from the first reactor, tail gas out also can enter the second reactor, and present in it, chlorine also will
Proceeding reaction, hydrogen chloride then goes successively to enter into the 3rd reactor by the way of tail gas, the like carry out continuously
Reaction, it is known that, react boring in the concentration of chlorinated paraffin will be gradually increased, the ratio of the paraffin oil of the inside existence is the most progressively
Reduce；Until, entering into the 4th reactor, its chlorine inlet pipeline is half above, thus reacts in the 4th reactor
Violent purity be decreased obviously, reaction is more prone to be controlled, and it is anti-persistently to proceed to the 6th with the reaction pattern of this gentleness
Answering still, during this, the chlorine in tail gas can fully be reacted, and accomplishes almost nil waste；
The temperature and pressure of detection reactor, the alarm when over-temp and over-pressure, first the chlorine of this reactor is regulated valve and close, when one
The while of in covering device during the most two or more generation overtemperature, cut off chlorine supply main valve；By be automatically adjusted recirculated water flow and
The feed rate of chlorine, it is possible to reasonably control supply and the saving of the energy of raw material, reach the effect of energy-conservation material-saving.
Finally collect for chlorinated paraffin finished product and the collection of tail gas processes, be chlorination from the 6th reactor tail gas almost all out
Hydrogen, by the duration of runs of switching value Valve controlling batch turning pump, and starts blowing still blowout hydrogen chloride feeding vent gas treatment
System.Concentration absorption by Hydrochloric Acid hydrogen chloride in the employing of absorption tower.The chlorine of unabsorbed trace, hydrochloric acid tail gas sequentially enter two-stage
Spray column, tail gas absorber, use low concentration acid and water to absorb, and final tail gas enters after Alkali absorption tower absorbs and is vented.Alkali absorption
Device obtains selling outside the solution barrelling containing 10% sodium hypochlorite after absorbing tail gas.Water is through absorbing hydrogen chloride step by step, and concentration of hydrochloric acid is gradually
Raise, finally give the hydrochloric acid that concentration is 30%, put into hydrochloric acid tank and store, sell.Containing that degassing still is advertised out is few
After the waste gas of amount hydrogen chloride enters tail gas absorber absorption, final tail gas enters after Alkali absorption tower absorbs and is vented；From the 6th reactor
Bottom release chlorinated paraffin finished product, send into chlorinated paraffin medial launder.
The above is only the preferred embodiment of the present invention, and protection scope of the present invention is not limited merely to above-described embodiment, all
The technical scheme belonged under thinking of the present invention belongs to protection scope of the present invention.It should be pointed out that, for the art is common
For technical staff, some improvements and modifications without departing from the principles of the present invention, these improvements and modifications also should be regarded as this
The protection domain of invention.
Claims (3)
1. efficiently utilizing a chlorinated paraffin continuous production processes for chlorine, including reactor group, this reactor group includes that first is anti-
Answer still to the 6th reactor, each reactor is fitted with uviol lamp, it is characterised in that each reactor is equipped with material
Cooling system, this cooling system includes out cooling down circulating line from the bottom of each reactor, has in this cooling circulating line
Product, this product enters the entrance of cooler, is cooled to 83-88 degree, then by the effect of circulating pump from top
Enter respective reactor；Reaction temperature controls to be 95-100 degree, and reaction pressure is 0.02-0.03Mpa；
Each reactor is equipped with respective pressure detecting and controls flow-route and temperature detection control technique, and pressure detecting controls technique；
Manual detection densimeter and electronic long-distance transmission densimeter are installed on the 4th reactor and the 6th reactor；
This production technology includes: paraffin oil enters the first reactor by paraffin oil entrance continuous print, and chlorine is from chlorine supply main
Respectively enteing in the chlorine inlet of each reactor, paraffin oil in the first reactor and chlorine, under the catalysis of ultraviolet light, enter
Row chlorination, and entered in the reactor of next stage by the upper level chlorination oil that obtains of reaction and paraffin oil mixture, even
Continuous reaction, the product that the 6th reactor obtains enters in chlorinated paraffin medial launder and collects；The hydrogen chloride of reaction generation and centre
The chlorine the being mingled with offgas outlet from the top of the reactor of previous stage enters into next stage reactor, and last 6th anti-
The tail gas answering still to obtain carries out general collection and enters engine manifold, is passed through exhaust treatment system and generates side-product；First reactor is extremely
A diameter of 4th reactor of the chlorine inlet pipeline of the 3rd reactor to the chlorine inlet pipeline of the 6th reactor diameter two
Times, corresponding chlorine supply flow control four reactor is to the half that the 6th reactor is the first reactor to the 3rd reactor.
The chlorinated paraffin continuous production processes efficiently utilizing chlorine the most according to claim 1, is characterized in that: the described 6th
Reactor is the refined of chlorinated paraffin, by the duration of runs of switching value Valve controlling batch turning pump, and starts blowing still blowout chlorine
Change hydrogen and send into exhaust treatment system, release chlorinated paraffin finished product from the bottom of the 6th reactor, send into chlorinated paraffin medial launder.
The chlorinated paraffin continuous production processes efficiently utilizing chlorine the most according to claim 2, is characterized in that: described tail gas
6th reactor tail gas out is sequentially sent to hydrogen chloride absorption tower, two-stage spray column, tail gas absorber and alkali and inhales by processing system
Receive tower, finally give byproduct hydrochloric acid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610626069.4A CN106010649A (en) | 2016-08-03 | 2016-08-03 | Chlorinated paraffin continuous production process efficiently utilizing chlorine gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610626069.4A CN106010649A (en) | 2016-08-03 | 2016-08-03 | Chlorinated paraffin continuous production process efficiently utilizing chlorine gas |
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| Publication Number | Publication Date |
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| CN106010649A true CN106010649A (en) | 2016-10-12 |
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| CN201610626069.4A Pending CN106010649A (en) | 2016-08-03 | 2016-08-03 | Chlorinated paraffin continuous production process efficiently utilizing chlorine gas |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
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| CN108275656A (en) * | 2017-08-31 | 2018-07-13 | 山东聊城鲁西化工第六化肥有限公司 | A kind of purifying plant and technique of hydrogen chloride as by product of chlorinated paraffin production gas |
| CN108360015A (en) * | 2018-04-19 | 2018-08-03 | 茌平信发华兴化工有限公司 | The production of caustic soda line of coproduction chlorinated paraffin and synthesis ammonia |
| CN109985589A (en) * | 2017-12-29 | 2019-07-09 | 黄国柱 | Irradiation reacts chemical industry processing system |
| CN110465161A (en) * | 2019-08-05 | 2019-11-19 | 潜江宜生新材料有限公司 | It is a kind of for producing the tail gas absorbing system of silane coupling agent |
| CN116393048A (en) * | 2023-06-07 | 2023-07-07 | 山东金城医药化工有限公司 | Continuous production system and production method of ethyl 4-chloro-2-methoxyiminoacetoacetate |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108275656A (en) * | 2017-08-31 | 2018-07-13 | 山东聊城鲁西化工第六化肥有限公司 | A kind of purifying plant and technique of hydrogen chloride as by product of chlorinated paraffin production gas |
| CN108275656B (en) * | 2017-08-31 | 2021-08-20 | 山东聊城鲁西化工第六化肥有限公司 | Device and process for purifying hydrogen chloride gas as byproduct of chlorinated paraffin |
| CN107694493A (en) * | 2017-09-20 | 2018-02-16 | 南京林业大学 | Multi-functional multiphase segmentation reaction unit and multiphase segmentation reaction method |
| CN107694493B (en) * | 2017-09-20 | 2023-07-14 | 南京林业大学 | Multifunctional multiphase sectional reaction device and multiphase sectional reaction method |
| CN109985589A (en) * | 2017-12-29 | 2019-07-09 | 黄国柱 | Irradiation reacts chemical industry processing system |
| CN108360015A (en) * | 2018-04-19 | 2018-08-03 | 茌平信发华兴化工有限公司 | The production of caustic soda line of coproduction chlorinated paraffin and synthesis ammonia |
| CN110465161A (en) * | 2019-08-05 | 2019-11-19 | 潜江宜生新材料有限公司 | It is a kind of for producing the tail gas absorbing system of silane coupling agent |
| CN116393048A (en) * | 2023-06-07 | 2023-07-07 | 山东金城医药化工有限公司 | Continuous production system and production method of ethyl 4-chloro-2-methoxyiminoacetoacetate |
| CN116393048B (en) * | 2023-06-07 | 2023-09-12 | 山东金城医药化工有限公司 | Continuous production system and production method of ethyl 4-chloro-2-methoxyiminoacetoacetate |
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