CN107759501A - A kind of device for producing DMDS coproduction dimethyltrisulfide - Google Patents
A kind of device for producing DMDS coproduction dimethyltrisulfide Download PDFInfo
- Publication number
- CN107759501A CN107759501A CN201711283696.3A CN201711283696A CN107759501A CN 107759501 A CN107759501 A CN 107759501A CN 201711283696 A CN201711283696 A CN 201711283696A CN 107759501 A CN107759501 A CN 107759501A
- Authority
- CN
- China
- Prior art keywords
- delivery pump
- connection
- dmds
- dimethyltrisulfide
- reactor
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- YWHLKYXPLRWGSE-UHFFFAOYSA-N Dimethyl trisulfide Chemical compound CSSSC YWHLKYXPLRWGSE-UHFFFAOYSA-N 0.000 title claims abstract description 79
- VLXBWPOEOIIREY-UHFFFAOYSA-N dimethyl diselenide Natural products C[Se][Se]C VLXBWPOEOIIREY-UHFFFAOYSA-N 0.000 title claims abstract description 54
- WQOXQRCZOLPYPM-UHFFFAOYSA-N dimethyl disulfide Chemical compound CSSC WQOXQRCZOLPYPM-UHFFFAOYSA-N 0.000 title claims abstract description 54
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 claims abstract description 64
- 238000006243 chemical reaction Methods 0.000 claims abstract description 43
- 238000004821 distillation Methods 0.000 claims abstract description 22
- 239000000463 material Substances 0.000 claims abstract description 7
- 230000007246 mechanism Effects 0.000 claims description 120
- 230000006835 compression Effects 0.000 claims description 13
- 238000007906 compression Methods 0.000 claims description 13
- 238000004073 vulcanization Methods 0.000 claims description 9
- 239000002912 waste gas Substances 0.000 claims description 6
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 239000000047 product Substances 0.000 abstract description 39
- 238000000034 method Methods 0.000 abstract description 15
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 12
- 238000004519 manufacturing process Methods 0.000 abstract description 12
- 239000005864 Sulphur Substances 0.000 abstract description 11
- 238000007670 refining Methods 0.000 abstract description 10
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 abstract description 6
- 229910000037 hydrogen sulfide Inorganic materials 0.000 abstract description 6
- 239000012535 impurity Substances 0.000 abstract description 4
- 239000007795 chemical reaction product Substances 0.000 abstract description 3
- 239000007791 liquid phase Substances 0.000 abstract 1
- 125000000118 dimethyl group Chemical group [H]C([H])([H])* 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 239000002994 raw material Substances 0.000 description 4
- 239000007789 gas Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000005951 Methiocarb Substances 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000007792 gaseous phase Substances 0.000 description 2
- 229910021645 metal ion Inorganic materials 0.000 description 2
- YFBPRJGDJKVWAH-UHFFFAOYSA-N methiocarb Chemical compound CNC(=O)OC1=CC(C)=C(SC)C(C)=C1 YFBPRJGDJKVWAH-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- QSLPNSWXUQHVLP-UHFFFAOYSA-N $l^{1}-sulfanylmethane Chemical compound [S]C QSLPNSWXUQHVLP-UHFFFAOYSA-N 0.000 description 1
- KYLIZBIRMBGUOP-UHFFFAOYSA-N Anetholtrithion Chemical group C1=CC(OC)=CC=C1C1=CC(=S)SS1 KYLIZBIRMBGUOP-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- PNVJTZOFSHSLTO-UHFFFAOYSA-N Fenthion Chemical compound COP(=S)(OC)OC1=CC=C(SC)C(C)=C1 PNVJTZOFSHSLTO-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000012190 activator Substances 0.000 description 1
- 239000003905 agrochemical Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 239000012043 crude product Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- XDNBJTQLKCIJBV-UHFFFAOYSA-N fensulfothion Chemical compound CCOP(=S)(OCC)OC1=CC=C(S(C)=O)C=C1 XDNBJTQLKCIJBV-UHFFFAOYSA-N 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 239000000796 flavoring agent Substances 0.000 description 1
- 235000019634 flavors Nutrition 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000002778 food additive Substances 0.000 description 1
- 235000013373 food additive Nutrition 0.000 description 1
- 235000013882 gravy Nutrition 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- QARBMVPHQWIHKH-UHFFFAOYSA-N methanesulfonyl chloride Chemical compound CS(Cl)(=O)=O QARBMVPHQWIHKH-UHFFFAOYSA-N 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 235000014347 soups Nutrition 0.000 description 1
- 238000005486 sulfidation Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
- 238000010257 thawing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C319/00—Preparation of thiols, sulfides, hydropolysulfides or polysulfides
- C07C319/22—Preparation of thiols, sulfides, hydropolysulfides or polysulfides of hydropolysulfides or polysulfides
- C07C319/24—Preparation of thiols, sulfides, hydropolysulfides or polysulfides of hydropolysulfides or polysulfides by reactions involving the formation of sulfur-to-sulfur bonds
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C319/00—Preparation of thiols, sulfides, hydropolysulfides or polysulfides
- C07C319/26—Separation; Purification; Stabilisation; Use of additives
- C07C319/28—Separation; Purification
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of method for producing DMDS coproduction dimethyltrisulfide, sulphur is mainly dissolved in DMDS solution by this method enters first reactor, sulphur and DMDS generate dimethyltrisulfide in reactor, dimethyltrisulfide and unreacted DMDS are introduced into first rectifying column and separated, tower top obtains DMDS product, the dimethyltrisulfide of bottom of towe can be used as production marketing, second reactor reaction generation DMDS can also be entered with methyl mercaptan, reaction solution enters the first flash tank removing hydrogen sulfide, liquid phase separates hydrogen sulfide and methyl mercaptan into Second distillation column tower top, materials at bottom of tower enters third distillation column, DMDS product is produced in rectifying column tower top, bottom of towe solution is recycled into first rectifying column isolated DMDS product again.The method that the present invention distinguishes refining spearation using reaction mass twice, two kinds of products of DMDS and dimethyltrisulfide can be obtained, it is reasonable with technological process configuration, equipment investment is small, good reaction selectivity, impurity content is low in reaction product, and refining spearation technique is simple, and product purity is high and easily controllable.
Description
Technical field
The present invention relates to production DMDS coproduction dimethyltrisulfide technical field, more particularly to a kind of production dimethyl
The device of two sulphur coproduction dimethyltrisulfides.
Background technology
DMDS DMDS is agricultural chemicals and dyestuff intermediate, is Entex, methiocarb mercaptodimethur, fensulfothion, methyl sulphur
Acid, the raw material of methylsufonyl chloride, in the oil industry as catalyst passivator, as ethene splits Jie's furnace coking inhibitor, hydrogenation takes off
Sulphur and the activator for giving sulfidation；Rubber liquid vulcanizing agent, curing agent DADMT raw materials and organic solvent.Dimethyltrisulfide master
It is used for medicine intermediate, is used on a small quantity as food additives in the food flavors such as gravy, soup class.DMDS and diformazan
Base trithio is all that market is well sold and in short supply, the long-term fine chemical product that supply falls short of demand.
In the relevant report and patent of methyl mercaptan vulcanization method production DMDS, mainly there are two kinds of production methods：One
Kind reacts generation DMDS for raw material sulphur and methyl mercaptan in vulcanization reaction device, and the material of reaction enters rectifying column
Refining spearation, this method methyl mercaptan and DMDS are lost in seriously, and refining spearation system process is complicated, and product yield is low, production
Product purity is not high.
One kind is two step vulcanization reactions, i.e. CN103864650A discloses a kind of method of continuous production DMDS,
Dimethyltrisulfide reactor is pumped into through charging after the thawing of raw material sulphur, the DMDS reaction generation dimethyl three with circulation
Sulphur, dimethyltrisulfide enter DMDS reactor, reaction generation DMDS, DMDS crude product with methyl mercaptan
Into knockout drum, most hydrogen sulfide is separated, liquid product enters rectifying column, overhead condensation recovery DMDS production
Product, hydrogen sulfide are discharged as fixed gas, and the DMDS and dimethyltrisulfide of tower reactor, which return, to be recycled, this method exist with
Lower deficiency：
1st, the material of end reaction enters separate unit rectifying column refining spearation, contains in the DMDS solution of such tower reactor circulation
Dimethyltrisulfide concentration it is higher, generate the sulphur of dimethyl four or more sulphur into dimethyltrisulfide reactor solution, cause mesh
It is low to mark product yield, refining spearation complex process.
2nd, the product to be reacted in dimethyltrisulfide reactor is the mixture of dimethyltrisulfide and DMDS,
Not sulfide hydrogen and methyl mercaptan, not by after mixture elder generation refining spearation, DMDS reactor is entered back into, causes dimethyl
Two reaction of Salmon-Saxl devices and refining separation device equipment investment are big, and the catalyst consumption amount of reaction also increases.
3rd, during rectifying tower reactor material Returning reactor, the heavy constituent accumulated in system, metal ion, salt etc.
It can not in time exclude, influence the purity and yield of DMDS product.
In presently disclosed patent of invention, not producing DMDS can be reported with the correlation of coproduction dimethyltrisulfide technology
Road.
The content of the invention
Present invention seek to address that the problem of above-mentioned technology is present, there is provided one kind production DMDS coproduction dimethyl three
The method of sulphur, there is technological process configuration rationally, equipment investment is small, good reaction selectivity, and reaction product impurity content is low, refines
The features such as separating technology is simple, and product purity is high and easily controllable.
A kind of device for producing DMDS coproduction dimethyltrisulfide, it is characterised in that including the first reaction mechanism,
Two reaction mechanisms and finished product collecting mechanism, in addition to vacuum mechanism, waste gas treatment mechanism, compression mechanism, methyl mercaptan addition mechanism,
Methyl mercaptan vulcanization mechanism, burn mechanism and methyl mercaptan combination mechanism, first reaction mechanism have four output ends respectively with institute
Stating finished product collecting mechanism, restructuring mechanism, vacuum mechanism and the connection of the second reaction mechanism, second reaction mechanism has four outputs
End is connected with the finished product collecting mechanism, burning mechanism, methyl mercaptan vulcanization mechanism and the first reaction mechanism respectively；
Further, first reaction mechanism include first reactor, first rectifying column, the first condenser, the first backflash,
First delivery pump, the second delivery pump and the 3rd delivery pump, the first reactor are provided with feed end, and material solution passes through charging
End enters in the first reactor, and the first reactor is connected with the first rectifying column, and the first rectifying column has three
Individual output end is connected with first condenser, second delivery pump and the 3rd delivery pump respectively, and first condenser has
Two output ends are connected with the vacuum mechanism and first backflash respectively, the vacuum mechanism and the exhaust gas processor
Structure is connected, and first backflash is connected with first delivery pump, and first delivery pump connects with the finished product collecting mechanism
Connect, the 3rd delivery pump is connected with the finished product collecting mechanism；
Further, second reaction mechanism include second reactor, the first flash tank, the 4th delivery pump, Second distillation column,
Second condenser, the second backflash, the 5th delivery pump, the second delivery pump, third distillation column, the 3rd backflash, the 3rd condenser,
7th delivery pump and the 8th delivery pump, the feed end of the second reactor are connected with the 3rd delivery pump, and described second is anti-
Two delivery ends of device are answered to be connected respectively with the compression mechanism and first flash tank, first flash tank there are two outputs
End is connected with the 4th delivery pump and the compression mechanism respectively, and the 4th delivery pump is connected with the Second distillation column,
The Second distillation column has two output ends to be connected respectively with second condenser and the 6th delivery pump, and described second is cold
Condenser has two output ends to be connected respectively with second backflash and the compression mechanism, second backflash and described the
Five delivery pumps are connected, and the 5th delivery pump is connected with the finished product collecting mechanism, the 6th delivery pump and the described 3rd essence
Tower connection is evaporated, the third distillation column has two output ends to be connected respectively with the 3rd backflash and the 8th delivery pump,
3rd backflash has two output ends to be connected respectively with the 3rd condenser and the burning mechanism, the 3rd condensation
Device is connected with the 7th delivery pump, and the 7th delivery pump is connected with the finished product collecting mechanism, the 8th delivery pump with
The first reactor connection；
Further, the methyl mercaptan combination mechanism and the methyl mercaptan addition mechanism be connecteds, the methyl mercaptan addition mechanism and
The feed end connection of the second reactor；
Further, second delivery pump is arranged on the first rectifying column bottom connection；
Further, choke valve is provided with the 3rd delivery pump, the 3rd conveying pump duty can be adjusted；
Further, the 8th rear pump is connected with the third distillation column bottom.
Have the advantage that：
The present invention can obtain DMDS and dimethyltrisulfide two using the method for the difference refining spearation of reaction mass twice
Kind product, technological process configuration is more reasonable, can be needed enter second reactor by adjusting dimethyltrisulfide according to production
Amount, any control obtains the yield of DMDS and dimethyltrisulfide product.It is small with equipment investment, reaction selectivity
Well, the features such as impurity content is low in reaction product, and refining spearation technique is simple, and product purity is high and easily controllable.
Brief description of the drawings
Fig. 1 is the process flow diagram of the present invention.
Wherein, 1 is the first reaction mechanism, and 2 be the second reaction mechanism, and 3 be finished product collecting mechanism, and 4 be vacuum mechanism, and 5 are
Waste gas treatment mechanism, 6 be compression mechanism, and 7 be that methyl mercaptan adds mechanism, and 8 be that methyl mercaptan vulcanizes mechanism, and 9 is burn mechanism, and 11 are
First reactor, 12 be first rectifying column, and 13 be the first condenser, and 14 be the first backflash, and 15 be the first delivery pump, and 16 be
Two delivery pumps, 17 be the 3rd delivery pump, and 21 be second reactor, and 22 be the first flash tank, and 23 be the 4th delivery pump, and 24 be second
Rectifying column, 25 be the second condenser, and 26 be the second backflash, and 27 be the 5th delivery pump, and 28 be the 6th delivery pump, and 29 be the 3rd essence
Tower is evaporated, 30 be the 3rd backflash, and 31 be the 3rd condenser, and 32 be the 7th delivery pump, and 33 be the 8th delivery pump.
Embodiment
A kind of device for producing DMDS coproduction dimethyltrisulfide, it is characterised in that including the first reaction mechanism 1,
Second reaction mechanism 2 and finished product collecting mechanism 3, in addition to vacuum mechanism 4, waste gas treatment mechanism 5, compression mechanism 6, methyl mercaptan add
Add mechanism 7, methyl mercaptan vulcanization mechanism 8, burn mechanism 9 and methyl mercaptan combination mechanism 10, first reaction mechanism 1 have four it is defeated
Go out end to be connected with the finished product collecting mechanism 3, restructuring mechanism, the reaction mechanism 2 of vacuum mechanism 4 and second respectively, described second is anti-
Mechanism 2 is answered there are four output ends anti-with the finished product collecting mechanism 3, burning mechanism 9, methyl mercaptan vulcanization mechanism 8 and first respectively
Mechanism 1 is answered to connect.
2nd, a kind of device for producing DMDS coproduction dimethyltrisulfide according to claim 1, its feature exist
In：First reaction mechanism 1 include first reactor 11, first rectifying column 12, the first condenser 13, the first backflash 14,
First delivery pump 15, the second delivery pump 16 and the 3rd delivery pump 17, the first reactor 11 are provided with feed end, material solution
Entered by feed end in the first reactor 11, the first reactor 11 is connected with the first rectifying column 12, described
First rectifying column 12 have three output ends respectively with first condenser 13, the delivery pump 17 of second delivery pump 16 and the 3rd
Connection, first condenser 13 have two output ends to be connected respectively with the vacuum mechanism 4 and first backflash 14, institute
State vacuum mechanism 4 to be connected with the waste gas treatment mechanism 5, first backflash 14 is connected with first delivery pump 15, institute
State the first delivery pump 15 to be connected with the finished product collecting mechanism 3, the 3rd delivery pump 17 connects with the finished product collecting mechanism 3
Connect.
3rd, a kind of device for producing DMDS coproduction dimethyltrisulfide according to claim 1, its feature exist
In：Second reaction mechanism 2 include second reactor 21, the first flash tank 22, the 4th delivery pump 23, Second distillation column 24,
Second condenser 25, the second backflash 26, the 5th delivery pump 27, the 6th delivery pump 28, third distillation column 29, the 3rd backflash
30th, the 3rd condenser 31, the 7th delivery pump 32 and the 8th delivery pump 33, the feed end of the second reactor 21 and the described 3rd
Delivery pump 17 connects, described 21 two delivery ends of second reactor respectively with the compression mechanism 6 and first flash tank 22
Connection, first flash tank 22 have two output ends to be connected respectively with the 4th delivery pump 23 and the compression mechanism 6, institute
State the 4th delivery pump 23 to be connected with the Second distillation column 24, the Second distillation column 24 there are two output ends respectively with described
Two condensers 25 and the 6th delivery pump 28 connect, second condenser 25 have two output ends respectively with described second time
Chute 26 and the compression mechanism 6 are connected, and second backflash 26 is connected with the 5th delivery pump 27, the 5th conveying
Pump 27 is connected with the finished product collecting mechanism 3, and the 6th delivery pump 28 is connected with the third distillation column 29, the 3rd essence
Evaporating tower 29 has two output ends to be connected respectively with the 3rd backflash 30 and the 8th delivery pump 33, the 3rd backflash
30 have two output ends to be connected respectively with the 3rd condenser 31 and the burning mechanism 9, the 3rd condenser 31 and institute
The 7th delivery pump 32 is stated to connect, the 7th delivery pump 32 is connected with the finished product collecting mechanism 3, the 8th delivery pump 33 with
The first reactor 11 connects.
4th, a kind of device for producing DMDS coproduction dimethyltrisulfide according to claim 1, its feature exist
In：The methyl mercaptan combination mechanism 10 and the methyl mercaptan addition mechanism 7 are connected, the methyl mercaptan addition mechanism 7 and described the
The feed end connection of two reactors 21.
5th, a kind of device for producing DMDS coproduction dimethyltrisulfide according to claim 2, its feature exist
In：Second delivery pump 16 is arranged on the bottom of first rectifying column 12 connection.
6th, a kind of device for producing DMDS coproduction dimethyltrisulfide according to claim 2, its feature exist
In：Choke valve is provided with 3rd delivery pump 17, the conveying capacity of the 3rd delivery pump 17 can be adjusted.
7th, a kind of device for producing DMDS coproduction dimethyltrisulfide according to claim 3, its feature exist
In：8th rear pump is connected with the bottom of third distillation column 29.
By the sulphur that quality is 600Kg, it is in 3525Kg DMDS solution, into first reactor to be dissolved in quality
11 excessive DMDSs and sulfur reaction, reaction generation dimethyltrisulfide quality：2362.5Kg and DMDS matter
Amount：1762.5Kg solution enters first rectifying column 12, is separated by the way of rectification under vacuum, top gaseous phase is cold through first
The condensation of condenser 13 enters the first backflash 14, and it is 1500Kg to obtain quality, and the DMDS product that purity is more than 99.5% passes through
First delivery pump 15 is sent into finished product stowage mechanism, and bottom of towe is by the restructuring lease making second containing metal ion, salt and other impurities
Delivery pump 16 is excluded in time, and the dimethyltrisulfide product that purity is 98% is obtained in the middle and lower part of first rectifying column 12, and quality is
2362.5Kg is sent into finished product collecting mechanism 3 or second reactor 21 through the pressure-raising of the 3rd delivery pump 17, is passed through according to production needs
The amount that dimethyltrisulfide enters second reactor 21 is adjusted, controls the production ratio of DMDS and dimethyltrisulfide product.
It is molten with the methyl mercaptan total overall reaction that quality is 1800Kg, reaction if DMDS product is fully entered in second reactor 21
Liquid enters the hydrogen sulfide 580Kg of the first flash tank 22 removing dissolving, and the solution after flash distillation enters the second essence through the 4th delivery pump 23
The top of tower 24, removed overhead hydrogen sulfide and micro methyl mercaptan are evaporated, bottom of towe solution enters third distillation column 29 through the 6th delivery pump 28
Middle part, top gaseous phase condense into the 3rd condenser 31, and fixed gas enters burning mechanism 9 and burned, and condensate liquid enters the 3rd backflow
Groove 30, the DMDS product purity that the 3rd backflash 30 comes out are sent into finished product through the 7th delivery pump 32 more than 99.5% and received
Collecting mechanism 3, bottom of towe solution are recycled into first rectifying column 12 through the 8th delivery pump 33 and separated again.
The invention is not limited in above-described embodiment, on the basis of technical scheme disclosed by the invention, the skill of this area
Art personnel are according to disclosed technology contents, it is not necessary to which performing creative labour can makes one to some of which technical characteristic
A little to replace and deform, these are replaced and deformation is within the scope of the present invention.
Claims (7)
1. a kind of device for producing DMDS coproduction dimethyltrisulfide, it is characterised in that including the first reaction mechanism（1）、
Second reaction mechanism（2）With finished product collecting mechanism（3）, in addition to vacuum mechanism（4）, waste gas treatment mechanism（5）, compression mechanism
（6）, methyl mercaptan addition mechanism（7）, methyl mercaptan vulcanization mechanism（8）, burn mechanism（9）With methyl mercaptan combination mechanism（10）, it is described
First reaction mechanism（1）Have four output ends respectively with the finished product collecting mechanism（3）, restructuring mechanism, vacuum mechanism（4）With
Two reaction mechanisms（2）Connection, second reaction mechanism（2）Have four output ends respectively with the finished product collecting mechanism（3）, burn
Burn mechanism（9）, methyl mercaptan vulcanization mechanism（8）With the first reaction mechanism（1）Connection.
A kind of 2. device for producing DMDS coproduction dimethyltrisulfide according to claim 1, it is characterised in that：Institute
State the first reaction mechanism（1）Including first reactor（11）, first rectifying column（12）, the first condenser（13）, the first backflash
（14）, the first delivery pump（15）, the second delivery pump（16）With the 3rd delivery pump（17）, the first reactor（11）Be provided with into
Expect end, material solution enters the first reactor by feed end（11）It is interior, the first reactor（11）With described first
Rectifying column（12）Connection, the first rectifying column（12）Have three output ends respectively with first condenser（13）, described
Two delivery pumps（16）With the 3rd delivery pump（17）Connection, first condenser（13）Have two output ends respectively with the vacuum
Mechanism（4）With first backflash（14）Connection, the vacuum mechanism（4）With the waste gas treatment mechanism（5）Connection, it is described
First backflash（14）With first delivery pump（15）Connection, first delivery pump（15）With the finished product collecting mechanism
（3）Connection, the 3rd delivery pump（17）With the finished product collecting mechanism（3）Connection.
A kind of 3. device for producing DMDS coproduction dimethyltrisulfide according to claim 1, it is characterised in that：Institute
State the second reaction mechanism（2）Including second reactor（21）, the first flash tank（22）, the 4th delivery pump（23）, Second distillation column
（24）, the second condenser（25）, the second backflash（26）, the 5th delivery pump（27）, the 6th delivery pump（28）, third distillation column
（29）, the 3rd backflash（30）, the 3rd condenser（31）, the 7th delivery pump（32）With the 8th delivery pump（33）, described second is anti-
Answer device（21）Feed end and the 3rd delivery pump（17）Connection, the second reactor（21）Two delivery ends respectively with institute
State compression mechanism（6）With first flash tank（22）Connection, first flash tank（22）Have two output ends respectively with institute
State the 4th delivery pump（23）With the compression mechanism（6）Connection, the 4th delivery pump（23）With the Second distillation column（24）
Connection, the Second distillation column（24）Have two output ends respectively with second condenser（25）With the 6th delivery pump
（28）Connection, second condenser（25）Have two output ends respectively with second backflash（26）With the compression mechanism
（6）Connection, second backflash（26）With the 5th delivery pump（27）Connection, the 5th delivery pump（27）With it is described into
Product collecting mechanism（3）Connection, the 6th delivery pump（28）With the third distillation column（29）Connection, the third distillation column
（29）Have two output ends respectively with the 3rd backflash（30）With the 8th delivery pump（33）Connection, the 3rd backflow
Groove（30）Have two output ends respectively with the 3rd condenser（31）With the burning mechanism（9）Connection, the 3rd condensation
Device（31）With the 7th delivery pump（32）Connection, the 7th delivery pump（32）With the finished product collecting mechanism（3）Connection, institute
State the 8th delivery pump（33）With the first reactor（11）Connection.
A kind of 4. device for producing DMDS coproduction dimethyltrisulfide according to claim 1, it is characterised in that：Institute
State methyl mercaptan combination mechanism（10）Mechanism is added with the methyl mercaptan（7）Connection, the methyl mercaptan add mechanism（7）With described
Two reactors（21）Feed end connection.
A kind of 5. device for producing DMDS coproduction dimethyltrisulfide according to claim 2, it is characterised in that：Institute
State the second delivery pump（16）It is arranged on the first rectifying column（12）Bottom connects.
A kind of 6. device for producing DMDS coproduction dimethyltrisulfide according to claim 2, it is characterised in that：Institute
State the 3rd delivery pump（17）It is interior to be provided with choke valve, the 3rd delivery pump can be adjusted（17）Conveying capacity.
A kind of 7. device for producing DMDS coproduction dimethyltrisulfide according to claim 3, it is characterised in that：Institute
State the 8th rear pump and the third distillation column（29）Bottom connects.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711283696.3A CN107759501A (en) | 2017-12-07 | 2017-12-07 | A kind of device for producing DMDS coproduction dimethyltrisulfide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711283696.3A CN107759501A (en) | 2017-12-07 | 2017-12-07 | A kind of device for producing DMDS coproduction dimethyltrisulfide |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107759501A true CN107759501A (en) | 2018-03-06 |
Family
ID=61277833
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711283696.3A Pending CN107759501A (en) | 2017-12-07 | 2017-12-07 | A kind of device for producing DMDS coproduction dimethyltrisulfide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107759501A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116651020A (en) * | 2023-07-31 | 2023-08-29 | 民勤县鑫达化工有限公司 | Separation device for dimethyl disulfide production and manufacturing and application method thereof |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1153160A (en) * | 1995-12-27 | 1997-07-02 | 西安近代化学研究所 | Production process of 1, 1, 1, 2-tetrafluoroethane |
| CN103864650A (en) * | 2014-03-20 | 2014-06-18 | 中国海洋石油总公司 | Method for continuously producing dimethyl disulfide |
| CN104592070A (en) * | 2015-01-13 | 2015-05-06 | 湖北兴发化工集团股份有限公司 | Preparation method of dimethyl disulfide |
| CN104610106A (en) * | 2015-01-13 | 2015-05-13 | 湖北兴发化工集团股份有限公司 | Method for producing dimethyl disulfide by using methyl mercaptan and sulfur vaporization method |
| CN107652159A (en) * | 2017-10-18 | 2018-02-02 | 山东华安新材料有限公司 | A kind of device and method for preparing 2,3,3,3 tetrafluoropropenes |
-
2017
- 2017-12-07 CN CN201711283696.3A patent/CN107759501A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1153160A (en) * | 1995-12-27 | 1997-07-02 | 西安近代化学研究所 | Production process of 1, 1, 1, 2-tetrafluoroethane |
| CN103864650A (en) * | 2014-03-20 | 2014-06-18 | 中国海洋石油总公司 | Method for continuously producing dimethyl disulfide |
| CN104592070A (en) * | 2015-01-13 | 2015-05-06 | 湖北兴发化工集团股份有限公司 | Preparation method of dimethyl disulfide |
| CN104610106A (en) * | 2015-01-13 | 2015-05-13 | 湖北兴发化工集团股份有限公司 | Method for producing dimethyl disulfide by using methyl mercaptan and sulfur vaporization method |
| CN107652159A (en) * | 2017-10-18 | 2018-02-02 | 山东华安新材料有限公司 | A kind of device and method for preparing 2,3,3,3 tetrafluoropropenes |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116651020A (en) * | 2023-07-31 | 2023-08-29 | 民勤县鑫达化工有限公司 | Separation device for dimethyl disulfide production and manufacturing and application method thereof |
| CN116651020B (en) * | 2023-07-31 | 2023-09-19 | 民勤县鑫达化工有限公司 | Separation device for dimethyl disulfide production and manufacturing and application method thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8389773B2 (en) | Cyclohexanone production process with impurities removal | |
| CN100532338C (en) | Method for producing benzyl chloride compound | |
| US8507729B2 (en) | Cyclohexanone production process with multiple post-distillation | |
| CN108840310B (en) | Device and process for producing hydrogen chloride by deep analysis from dilute hydrochloric acid | |
| US20200369637A1 (en) | System and Method for Continuously Preparing Furfural Using Lignocellulosic Raw Material | |
| WO2014001461A1 (en) | Process for the production of a mixture comprising cyclohexanone and cyclohexanol from phenol | |
| CN111574329B (en) | Reactive distillation device and method for producing 4-chloro-3, 5-dimethylphenol | |
| CN101781164B (en) | Preparation method of difluoromono-chloroethane | |
| CN106892792B (en) | Continuous synthesis method and equipment of 3, 4-dichloro benzotrifluoride | |
| CN107759501A (en) | A kind of device for producing DMDS coproduction dimethyltrisulfide | |
| CN102992985A (en) | Method and device for separating and recycling butanone by three-tower pressure-variable rectification and heat integration | |
| CN114835564B (en) | Method for producing photoinitiator UV-1173 by condensation method | |
| CN114835569B (en) | Method for producing photoinitiator UV-184 by condensation method | |
| CA2896706C (en) | Urea plant revamping method | |
| CN112047834A (en) | Device and method for continuously preparing isobutyric anhydride | |
| CN101328129B (en) | Preparation of 3-methoxy propanamine | |
| CN101328130B (en) | Preparation of 2-ethoxy ethyl amine | |
| CN211546374U (en) | Device for producing dimethyl disulfide and dimethyl trisulfide | |
| CN106928105A (en) | One-step method continuously produces the Processes and apparatus of DMDS | |
| CN116023257B (en) | Continuous production method of high-purity propionyl chloride | |
| CN216005719U (en) | System device for continuously preparing trans-1, 3-dichloropropene | |
| CN218834066U (en) | Novel separation system for acrylic acid device | |
| CN112694639B (en) | Method and device for purifying polymerization liquid in EVOH production process | |
| CN114436843B (en) | Method for continuously producing dimethyl adipate from cyclohexane | |
| CN113056458B (en) | Production of hydroxyethyl piperazine |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information | ||
| CB02 | Change of applicant information |
Address after: 570000 No. a5002-323, A1 area, Fuxing City, 32 Binhai Avenue, Longhua District, Haikou City, Hainan Province Applicant after: Chadu (Hainan) Technology Co.,Ltd. Address before: Part 541, 5A / F, building B, 155 Fute West 1st Road, China (Shanghai) pilot Free Trade Zone, Pudong New Area, Shanghai Applicant before: CHADU (SHANGHAI) TECHNOLOGY Co.,Ltd. |
|
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20180306 |