CN202936335U - Cleaner production method and device for dinitrotoluene - Google Patents

Cleaner production method and device for dinitrotoluene Download PDF

Info

Publication number
CN202936335U
CN202936335U CN2012204776130U CN201220477613U CN202936335U CN 202936335 U CN202936335 U CN 202936335U CN 2012204776130 U CN2012204776130 U CN 2012204776130U CN 201220477613 U CN201220477613 U CN 201220477613U CN 202936335 U CN202936335 U CN 202936335U
Authority
CN
China
Prior art keywords
nitric acid
dinitrotoluene
dnt
storage tank
microreactor
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.)
Expired - Fee Related
Application number
CN2012204776130U
Other languages
Chinese (zh)
Inventor
张洪林
王东伟
刘宝民
吕文方
缪成蛟
全树新
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
LIAONING QINGYANG SPECIAL CHEMICAL CO Ltd
Original Assignee
LIAONING QINGYANG SPECIAL CHEMICAL CO Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by LIAONING QINGYANG SPECIAL CHEMICAL CO Ltd filed Critical LIAONING QINGYANG SPECIAL CHEMICAL CO Ltd
Priority to CN2012204776130U priority Critical patent/CN202936335U/en
Application granted granted Critical
Publication of CN202936335U publication Critical patent/CN202936335U/en
Anticipated expiration legal-status Critical
Expired - Fee Related legal-status Critical Current

Links

Classifications

    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/10Process efficiency

Abstract

The utility model relates to a cleaner production method and a cleaner production device for dinitrotoluene and belongs to the field of chemical process. The cleaning process method for preparing dinitrotoluene is implemented by adopting a toluene micro-reactor nitration process, a separation process of a fiber bed liquid phase separator for mixture of nitric acid and dinitrotoluene, and a dilute nitric acid thickening and concentration process. The device comprises a micro-reactor, a fiber bed separator, a mixing tank, an autoclave, a cooler, a bleaching tower, a concentrating tower, a condenser, a nitric acid storage tank, a conveying pump, a magnesium sulphate storage tank and an evaporator; and the micro-reactor is used for accomplish nitration reaction, is formed by connecting a plurality of micro-pipes in parallel, has a very large specific surface area and forms a continuous production procedure, so that favorable heat exchange efficiency and mixing efficiency can be achieved, the reaction temperature can be controlled accurately, reaction materials can be mixed instantly according to an accurate ratio, the yield, the selectivity and the security are improved, and the reaction time can be shortened.

Description

A kind of clean preparation method of dinitrotoluene (DNT) and device
Technical field
The utility model relates to a kind of clean preparation method and device of dinitrotoluene (DNT), belongs to the chemical technique field.
Background technology
Tolylene diisocyanate is called for short TDI, mainly for the production of urethane foam.Be used widely because urethane foam has good performance, market demand constantly increases, and the main raw material dinitrotoluene (DNT) that causes making tolylene diisocyanate and be TDI is that the demand of DNT also constantly increases.
At present, the DNT industrial production generally adopts the production technique of nitric-sulfuric acid nitration of toluene, produces a large amount of nitric-sulfuric acids in production and need to carry out concentration, when dilute sulphuric acid concentration too low (lower than 40%), if recycle, the concentration process need consumes mass energy, cost recovery is high; If do not reclaim to get rid of with waste water and can cause serious environmental pollution.
Nitration reaction is used reactor usually, and the batch production operation of reactor can cause the nitration reaction overlong time, thereby causes the production process time of whole dinitrotoluene (DNT) long.
Principle is seen document " nitrated theory " Lv Chunxu, Jiangsu science tech publishing house, in October, 1993 first version.
The utility model content
The purpose of this utility model is that in prior art, the nitric-sulfuric acid recovery needs to consume mass energy, cost recovery is high in order to solve, and does not cause serious environmental pollution if do not reclaim; And the application response still carries out long problem of time used when nitrated, has proposed a kind of clean preparation method and device of dinitrotoluene (DNT).
The purpose of this utility model realizes by following technical proposals:
A kind of clean preparation method of dinitrotoluene (DNT), concrete steps are as follows:
Step 1, nitrated
Toluene and concentration are not less than 90% nitric acid as raw material, are under the condition of 1:5~10 at toluene and nitric acid feed ratio, carry out nitration reaction by microreactor, make the thick mixing solutions of dinitrotoluene (DNT) and rare nitric acid; Toluene and nitric acid are put into microreactor, after adopting the microreactor technology to carry out the nitric acid nitrating of toluene, obtain DNT, HNO 3And H 2The mixing solutions of O;
The chemical equation of producing dinitrotoluene (DNT) with nitric acid nitrating toluene is:
C 6H 5CH 3+2HNO 3=C 6H 3CH 3(NO 2) 2+2H 2O
Step 2, separation
The thick mixing solutions of the dinitrotoluene (DNT) of step 1 gained and rare nitric acid under the condition of 55 ℃~70 ℃, is separated with rare nitric acid dinitrotoluene (DNT) by fibre bed liquid liquid phase separator, obtain dinitrotoluene (DNT) product and rare nitric acid;
Step 3, enrichment and concentrated
According to using needs to carry out enrichment or concentrated to rare nitric acid;
Rare nitric acid enrichment technology
With liquid N 2O 4Mix with rare nitric acid, send into autoclave, pass into oxygen, liquid N 2O 4, the water direct reaction in autoclave in oxygen and rare nitric acid generates concentrated nitric acid; Chemical equation is:
2N 2O 4+2H 2O+O 2=4HNO 3+59kJ
The concentrated nitric acid that makes contains free NO 2And present yellow, and need carry out bleaching, concentrated nitric acid is sent into bleaching tower, pass into air, free NO 2Blow out, obtain 97% finished product concentrated nitric acid, because reaction process is thermopositive reaction, the NO that blows out 2Need to send back to autoclave after water cooler is cooling.
Rare nitric acid concentration technique
Rare nitric acid and magnesium nitrate solution are joined in upgrading tower, and the concentrated nitric acid steam after the collection condenser condenses namely obtains concentrated nitric acid solution; Density loss after the magnesium nitrate solution suction, recycling after can concentrating by evaporator evaporation.
The described concentration of nitric acid of step 1 is preferred 97%, and toluene and nitric acid feed ratio are preferably 1:8;
The described autoclave pressure 5.0MPa of step 3.
The described magnesium nitrate solution concentration 70%~80% of step 3.
A kind of cleaning production apparatus of dinitrotoluene (DNT) comprises: microreactor, fibre bed separator, tempering tank, autoclave, water cooler, bleaching tower, upgrading tower, condenser, nitric acid storage tank, transferpump, sal epsom storage tank, vaporizer;
Its annexation is: the nitric acid storage tank is connected with microreactor by transferpump, and toluene and nitric acid enter microreactor from the microreactor feeding end; The microreactor discharge end is connected with fibre bed liquid liquid/gas separator, and fibre bed liquid liquid/gas separator discharge port connects respectively the DNT product and receives pipeline and tempering tank; Tempering tank is connected with upgrading tower with autoclave respectively; Autoclave is provided with N 2O 4, oxygen intake, water cooler access port; Bleaching tower is provided with liquid material entrance, liquid material outlet, the outlet of gas material; The autoclave exit end connects bleaching tower liquid material entrance, and the outlet of bleaching tower liquid material connects the nitric acid storage tank, and the outlet of bleaching tower gas material connects water cooler, and the water cooler the other end is connected with autoclave; Upgrading tower is provided with discharge port, vapour outlet; The upgrading tower discharge port connects condenser one end, and the condenser the other end connects the nitric acid storage tank, and vapour outlet connects vaporizer, and the vaporizer end connects the magnesium nitrate solution storage tank, and the magnesium nitrate solution storage tank is connected with upgrading tower through transferpump;
Microreactor, fibre bed liquid liquid/gas separator, tempering tank, nitric acid storage tank, autoclave, water cooler, bleaching tower consist of circulation loop, realize the cleaner production of dinitrotoluene (DNT), and the rare nitric acid that produces in production process is carried out the enrichment recycling.
Its working process is: with toluene and nitric acid after metering, input microreactor with transferpump respectively, both mixtures are completed nitration reaction in the flow process of microreactor, and reacted product is for containing DNT, HNO 3And H 2The mixture of O; Mixture enters fibre bed liquid liquid phase separator, through the drop multiplication, the different dinitrotoluene (DNT) of density is separated with rare nitric acid, and the dinitrotoluene (DNT) after separation is that DNT sends into product library; Rare nitric acid of separating is carried out enrichment, at first with liquid N 2O 4Be transported to autoclave, rarer nitric acid is transported to autoclave, both pass into oxygen after mixing.Liquid N 2O 4, to generate concentration be 97% concentrated nitric acid to the water direct reaction in autoclave in oxygen and rare nitric acid.The concentrated nitric acid that makes contains free NO 2And present yellow, and need carry out bleaching, concentrated nitric acid is sent into bleaching tower, pass into air, free NO 2Blow out, because reaction process produces heat, NO 2Gas material outlet through bleaching tower top is transported to water cooler, through cooled NO 2Send autoclave back to.
Microreactor, fibre bed liquid liquid/gas separator, tempering tank, nitric acid storage tank, upgrading tower, condenser, vaporizer consist of another circulation loop, realize the cleaner production of dinitrotoluene (DNT), and the rare nitric acid that produces in production process is carried out the concentration and recovery recycling.
Its working process is: with toluene and nitric acid after metering, input microreactor with transferpump respectively, both mixtures are completed nitration reaction in the flow process of microreactor, and reacted product is for containing DNT, HNO 3And H 2The mixture of O; Mixture enters fibre bed liquid liquid phase separator, through the drop multiplication, the different dinitrotoluene (DNT) of density is separated with rare nitric acid, and the dinitrotoluene (DNT) after separation is that DNT sends into product library; Rare nitric acid of separating is concentrated, rare nitric acid is joined in upgrading tower and the magnesium nitrate solution reaction, the concentrated nitric acid steam that upgrading tower top generates enters condenser, and the nitric acid of condensation is admitted to storage tank.The magnesium nitrate solution with crossing that contains excessive water is drawn from the bottom of tower, enters vaporizer, and the magnesium nitrate solution that steams moisture sends back to upgrading tower again and recycles.
Beneficial effect
1, the clean preparation method of a kind of dinitrotoluene (DNT) of the present utility model adopts nitric acid nitrating toluene to generate dinitrotoluene (DNT), does not use the mixing acid of nitric acid and sulfuric acid, there is no the generation of dilute sulphuric acid.
2, the clean preparation method of a kind of dinitrotoluene (DNT) of the present utility model, rare nitric acid can be recycled by enrichment and concentration technology, economize on resources, and recovery process is simple.
3, the clean preparation method of a kind of dinitrotoluene (DNT) of the present utility model, utilize microreactor to complete nitration reaction, microreactor is formed in parallel by a lot of microtubules, great specific surface area is arranged, form the continous way production process, so it has good heat exchange efficiency and mixing efficiency, can accurately control temperature of reaction and reaction mass by the instantaneous mixing of accurate proportioning, improve yield, selectivity, security, reduce the reaction times; The batch reactor and the microreactor nitrifying process residence time of material that reach identical nitration reaction effect are respectively greater than 1 hour with less than 10 seconds, and microreactor is Reaction time shorten significantly; Test shows, when temperature is 60 °, mass concentration is that 97% nitric acid mixes according to 8:1 with the toluene ratio, the mass concentration that obtains dinitrotoluene (DNT) through traditional reactor reaction is 85%, yield is 87%, and the mass concentration that obtains dinitrotoluene (DNT) through the microreactor reaction is 98.8%, and yield is 94%, this shows that little reaction more is applicable to suitability for industrialized production with respect to traditional kettle type nitration technique.
Description of drawings
Fig. 1 is dinitrotoluene (DNT) process for cleanly preparing schema;
Fig. 2 is the microreactor structural representation.
Wherein, 1-microreactor, 2-fibre bed liquid liquid/gas separator, 3-tempering tank, 4-autoclave, 5-water cooler, 6-bleaching tower, 7-upgrading tower, 8-condenser, 9-nitric acid storage tank, 10-transferpump, 11-sal epsom storage tank, 12-vaporizer.
Embodiment
Embodiment 1
A kind of dinitrotoluene (DNT) clean preparation method, concrete steps are as follows:
Step 1, nitrated
Be that 90% nitric acid is as raw material with toluene and concentration, be under the condition of 1:5 at toluene and nitric acid feed ratio, carry out nitration reaction by microreactor 1, microreactor 1 structural representation as shown in Figure 2, the residence time of material in microreactor 1 is controlled at 8s, temperature of reaction: 58 ℃, obtain DNT, HNO after nitrated 3And H 2The mixing solutions of O;
Step 2, separation
With the thick mixing solutions of the dinitrotoluene (DNT) of step 1 gained and rare nitric acid under the condition of 55 ℃, by fibre bed liquid liquid phase separator, dinitrotoluene (DNT) is separated with rare nitric acid, obtain dinitrotoluene (DNT) product and rare nitric acid, measuring the dinitrotoluene (DNT) product purity is 94.6%, yield 92%, rare concentration of nitric acid of generation is 86.41%;
Step 3, enrichment or concentrated
According to using needs to carry out enrichment to rare nitric acid.With liquid N 2O 4Mix with rare nitric acid, send into autoclave 4, set autoclave 4 pressure 5.0Mpa, pass into oxygen, liquid N 2O 4, the water in oxygen and rare nitric acid generates concentrated nitric acid at the interior direct reaction of autoclave 4, and measuring its concentration is 97%.
A kind of cleaning production apparatus of dinitrotoluene (DNT), comprise: microreactor 1, fibre bed separator, tempering tank 3, autoclave 4, water cooler 5, bleaching tower 6, upgrading tower 7, condenser 8, nitric acid storage tank 9, transferpump 10, sal epsom storage tank 11, vaporizer 12, as shown in Figure 1;
Its annexation is: nitric acid storage tank 9 is connected with microreactor 1 by transferpump 10, and toluene and nitric acid enter microreactor 1 from microreactor 1 feeding end; Microreactor 1 discharge end is connected with fibre bed liquid liquid/gas separator 2, and fibre bed liquid liquid/gas separator 2 discharge ports connect respectively the DNT product and receive pipeline and tempering tank 3; Tempering tank 3 is connected with upgrading tower 7 with autoclave 4 respectively; Autoclave 4 is provided with N 2O 4, oxygen intake, water cooler 5 access ports; Bleaching tower 6 is provided with liquid material entrance, liquid material outlet, the outlet of gas material; Autoclave 4 exit end connect bleaching tower 6 liquid material entrances, and bleaching tower 6 liquid material outlets connect nitric acid storage tank 9, and bleaching tower 6 gas material outlets connect water cooler 5, and water cooler 5 the other ends are connected with autoclave 4; Upgrading tower 7 is provided with discharge port, vapour outlet; Upgrading tower 7 discharge ports connect condenser 8 one ends, and condenser 8 the other ends connect nitric acid storage tank 9, and vapour outlet connects vaporizer 12, and vaporizer 12 ends connect the magnesium nitrate solution storage tank, and the magnesium nitrate solution storage tank is connected with upgrading tower 7 through transferpump 10;
Microreactor 1, fibre bed liquid liquid/gas separator 2, tempering tank 3, nitric acid storage tank 9, autoclave 4, water cooler 5, bleaching tower 6 consist of circulation loop, realize the cleaner production of dinitrotoluene (DNT), and the rare nitric acid that produces in production process is carried out the enrichment recycling.
Microreactor 1, fibre bed liquid liquid/gas separator 2, tempering tank 3, nitric acid storage tank 9, upgrading tower 7, condenser 8, vaporizer 12 consist of another circulation loop, realize the cleaner production of dinitrotoluene (DNT), and the rare nitric acid that produces in production process is carried out the concentration and recovery recycling.
Embodiment 2
A kind of dinitrotoluene (DNT) clean preparation method, concrete steps are as follows:
Step 1, nitrated
Be that 93% nitric acid is as raw material with toluene and concentration, be under the condition of 1:6 at toluene and nitric acid feed ratio, carry out nitration reaction by microreactor 1, the residence time of material in microreactor 1 is controlled at 10s, temperature of reaction: 60 ℃, obtain DNT, HNO after nitrated 3And H 2The mixing solutions of O;
Step 2, separation
With the thick mixing solutions of the dinitrotoluene (DNT) of step 1 gained and rare nitric acid under the condition of 57 ℃, by fibre bed liquid liquid phase separator, dinitrotoluene (DNT) is separated with rare nitric acid, obtain dinitrotoluene (DNT) product and rare nitric acid, measuring the dinitrotoluene (DNT) product purity is 95.6%, yield 93%, rare concentration of nitric acid of generation is 88.51%;
Step 3, enrichment or concentrated
According to using needs that rare nitric acid is concentrated.Be that 75% magnesium nitrate solution joins in upgrading tower 7 with rare nitric acid and concentration, collect the condensed concentrated nitric acid steam of condenser 8, obtain concentrated nitric acid solution, measuring concentration is 96.7%; Density loss after the magnesium nitrate solution suction can be by recycling after vaporizer 12 evaporation concentration.
Embodiment 3
A kind of dinitrotoluene (DNT) clean preparation method, concrete steps are as follows:
Step 1, nitrated
Be that 95% nitric acid is as raw material with toluene and concentration, be under the condition of 1:7 at toluene and nitric acid feed ratio, carry out nitration reaction by microreactor 1, the residence time of material in microreactor 1 is controlled at 12s, temperature of reaction: 60 ℃, obtain DNT, HNO after nitrated 3And H 2The mixing solutions of O;
Step 2, separation
With the thick mixing solutions of the dinitrotoluene (DNT) of step 1 gained and rare nitric acid under the condition of 58 ℃, by fibre bed liquid liquid phase separator, dinitrotoluene (DNT) is separated with rare nitric acid, obtain dinitrotoluene (DNT) product and rare nitric acid, measuring the dinitrotoluene (DNT) product purity is 91.2%, yield 91%, rare concentration of nitric acid of generation is 89.92%;
Step 3, enrichment or concentrated
According to using needs to carry out enrichment to rare nitric acid.With liquid N 2O 4Mix with rare nitric acid, send into autoclave 4, set autoclave 4 pressure 6.0Mpa, pass into oxygen, liquid N 2O 4, the water in oxygen and rare nitric acid generates concentrated nitric acid at the interior direct reaction of autoclave 4, and measuring its concentration is 97%.
Embodiment 4
A kind of dinitrotoluene (DNT) clean preparation method, concrete steps are as follows:
Step 1, nitrated
Be that 97% nitric acid is as raw material with toluene and concentration, be under the condition of 1:8 at toluene and nitric acid feed ratio, carry out nitration reaction by microreactor 1, the residence time of material in microreactor 1 is controlled at 15s, temperature of reaction: 60 ℃, obtain DNT, HNO after nitrated 3And H 2The mixing solutions of O;
Step 2, separation
With the thick mixing solutions of the dinitrotoluene (DNT) of step 1 gained and rare nitric acid under the condition of 70 ℃, by fibre bed liquid liquid phase separator, dinitrotoluene (DNT) is separated with rare nitric acid, obtain dinitrotoluene (DNT) product and rare nitric acid, measuring the dinitrotoluene (DNT) product purity is 95%, yield 94%, rare concentration of nitric acid of generation is 90.92%;
Step 3, enrichment or concentrated
According to using needs that rare nitric acid is concentrated.Be that 80% magnesium nitrate solution joins in upgrading tower 7 with rare nitric acid and concentration, collect the condensed concentrated nitric acid steam of condenser 8, obtain concentrated nitric acid solution, measuring concentration is 95.5%; Density loss after the magnesium nitrate solution suction can be by recycling after vaporizer 12 evaporation concentration.
Embodiment 5
A kind of dinitrotoluene (DNT) clean preparation method, concrete steps are as follows:
Step 1, nitrated
Be that 97% nitric acid is as raw material with toluene and concentration, be under the condition of 1:9 at toluene and nitric acid feed ratio, carry out nitration reaction by microreactor 1, the residence time of material in microreactor 1 is controlled at 20s, temperature of reaction: 62 ℃, obtain DNT, HNO after nitrated 3And H 2The mixing solutions of O;
Step 2, separation
With the thick mixing solutions of the dinitrotoluene (DNT) of step 1 gained and rare nitric acid under the condition of 65 ℃, by fibre bed liquid liquid phase separator, dinitrotoluene (DNT) is separated with rare nitric acid, obtain dinitrotoluene (DNT) product and rare nitric acid, measuring the dinitrotoluene (DNT) product purity is 92%, yield 90%, rare concentration of nitric acid of generation is 91.68%;
Step 3, enrichment or concentrated
According to using needs to carry out enrichment to rare nitric acid.With liquid N 2O 4Mix with rare nitric acid, send into autoclave 4, set autoclave 4 pressure 5.0Mpa, pass into oxygen, liquid N 2O 4, the water in oxygen and rare nitric acid generates concentrated nitric acid at the interior direct reaction of autoclave 4, and measuring its concentration is 97%.
Embodiment 6
A kind of dinitrotoluene (DNT) clean preparation method, concrete steps are as follows:
Step 1, nitrated
Be that 96% nitric acid is as raw material with toluene and concentration, be under the condition of 1:10 at toluene and nitric acid feed ratio, carry out nitration reaction by microreactor 1, the residence time of material in microreactor 1 is controlled at 16s, temperature of reaction: 59 ℃, obtain DNT, HNO after nitrated 3And H 2The mixing solutions of O;
Step 2, separation
With the thick mixing solutions of the dinitrotoluene (DNT) of step 1 gained and rare nitric acid under the condition of 70 ℃, by fibre bed liquid liquid phase separator, dinitrotoluene (DNT) is separated with rare nitric acid, obtain dinitrotoluene (DNT) product and rare nitric acid, measuring the dinitrotoluene (DNT) product purity is 95%, yield 87%, rare concentration of nitric acid of generation is 92.27%;
Step 3, enrichment or concentrated
According to using needs that rare nitric acid is concentrated.Be that 75% magnesium nitrate solution joins in upgrading tower 7 with rare nitric acid and concentration, collect the condensed concentrated nitric acid steam of condenser 8, obtain concentrated nitric acid solution, measuring concentration is 96%; Density loss after the magnesium nitrate solution suction can be by recycling after vaporizer 12 evaporation concentration.

Claims (1)

1. the cleaning production apparatus of a dinitrotoluene (DNT), comprising: microreactor (1), fibre bed separator, tempering tank (3), autoclave (4), water cooler (5), bleaching tower (6), upgrading tower (7), condenser (8), nitric acid storage tank (9), transferpump (10), sal epsom storage tank (11), vaporizer (12); Nitric acid storage tank (9) is connected with microreactor (1) by transferpump (10), and toluene and nitric acid enter microreactor (1) from microreactor (1) feeding end; Microreactor (1) discharge end is connected with fibre bed liquid liquid/gas separator (2), and fibre bed liquid liquid/gas separator (2) discharge port connects respectively the DNT product and receives pipeline and tempering tank (3); Tempering tank (3) is connected with upgrading tower (7) with autoclave (4) respectively; Autoclave (4) is provided with N 2O 4, oxygen intake, water cooler (5) access port; Bleaching tower (6) is provided with liquid material entrance, liquid material outlet, the outlet of gas material; Autoclave (4) exit end connects bleaching tower (6) liquid material entrance, the outlet of bleaching tower (6) liquid material connects nitric acid storage tank (9), the outlet of bleaching tower (6) gas material connects water cooler (5), and water cooler (5) the other end is connected with autoclave (4); Upgrading tower (7) is provided with discharge port, vapour outlet; Upgrading tower (7) discharge port connects condenser (8) one ends, condenser (8) the other end connects nitric acid storage tank (9), vapour outlet connects vaporizer (12), vaporizer (12) end connects the magnesium nitrate solution storage tank, and the magnesium nitrate solution storage tank is connected with upgrading tower (7) through transferpump (10); Microreactor (1), fibre bed liquid liquid/gas separator (2), tempering tank (3), nitric acid storage tank (9), autoclave (4), water cooler (5), bleaching tower (6) consist of circulation loop, realize the cleaner production of dinitrotoluene (DNT), and the rare nitric acid that produces in production process is carried out the enrichment recycling; Microreactor (1), fibre bed liquid liquid/gas separator (2), tempering tank (3), nitric acid storage tank (9), upgrading tower (7), condenser (8), vaporizer (12) consist of another circulation loop, realize the cleaner production of dinitrotoluene (DNT), and the rare nitric acid that produces in production process is carried out the concentration and recovery recycling.
CN2012204776130U 2012-09-19 2012-09-19 Cleaner production method and device for dinitrotoluene Expired - Fee Related CN202936335U (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN2012204776130U CN202936335U (en) 2012-09-19 2012-09-19 Cleaner production method and device for dinitrotoluene

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN2012204776130U CN202936335U (en) 2012-09-19 2012-09-19 Cleaner production method and device for dinitrotoluene

Publications (1)

Publication Number Publication Date
CN202936335U true CN202936335U (en) 2013-05-15

Family

ID=48320587

Family Applications (1)

Application Number Title Priority Date Filing Date
CN2012204776130U Expired - Fee Related CN202936335U (en) 2012-09-19 2012-09-19 Cleaner production method and device for dinitrotoluene

Country Status (1)

Country Link
CN (1) CN202936335U (en)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102838489A (en) * 2012-09-19 2012-12-26 辽宁庆阳特种化工有限公司 Clean production method and device of dinitrotoluene
CN107814368A (en) * 2017-10-31 2018-03-20 湖北东方化工有限公司 The device of dust technology produced by a kind of nitrotoleune Waste Sulfuric Acid using absorption tower processing
CN107814366A (en) * 2017-10-31 2018-03-20 湖北东方化工有限公司 A kind of micro- cost of nitrotoleune sulfur waste acid treatment low concentration dust technology improves the production method of concentration
CN107892285A (en) * 2017-10-31 2018-04-10 湖北东方化工有限公司 A kind of method of dust technology produced by nitrotoleune Waste Sulfuric Acid using absorption tower processing
CN111018715A (en) * 2019-12-14 2020-04-17 中国科学院大连化学物理研究所 Microchannel synthesis method of dinitrobenzene

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102838489A (en) * 2012-09-19 2012-12-26 辽宁庆阳特种化工有限公司 Clean production method and device of dinitrotoluene
CN107814368A (en) * 2017-10-31 2018-03-20 湖北东方化工有限公司 The device of dust technology produced by a kind of nitrotoleune Waste Sulfuric Acid using absorption tower processing
CN107814366A (en) * 2017-10-31 2018-03-20 湖北东方化工有限公司 A kind of micro- cost of nitrotoleune sulfur waste acid treatment low concentration dust technology improves the production method of concentration
CN107892285A (en) * 2017-10-31 2018-04-10 湖北东方化工有限公司 A kind of method of dust technology produced by nitrotoleune Waste Sulfuric Acid using absorption tower processing
CN107892285B (en) * 2017-10-31 2020-06-09 湖北东方化工有限公司 Method for treating dilute nitric acid generated by nitrotoluene waste sulfuric acid by using absorption tower
CN107814366B (en) * 2017-10-31 2020-06-09 湖北东方化工有限公司 Production method for slightly increasing concentration of low-concentration dilute nitric acid treated by nitrotoluene waste sulfuric acid
CN107814368B (en) * 2017-10-31 2020-06-09 湖北东方化工有限公司 Utilize absorption tower to handle device of produced dilute nitric acid of nitrotoluene waste sulfuric acid
CN111018715A (en) * 2019-12-14 2020-04-17 中国科学院大连化学物理研究所 Microchannel synthesis method of dinitrobenzene

Similar Documents

Publication Publication Date Title
CN102838489B (en) Clean production method and device of dinitrotoluene
CN202936335U (en) Cleaner production method and device for dinitrotoluene
CN103304420A (en) Clean preparation method of 2, 4-dichloro-3, 5-dinitrobenzotrifluoride
CN102329253A (en) Reaction apparatus for resorcinol neutralization reaction section and reaction technology thereof
CN102976904B (en) Preparation device of isobutyl vinyl ether and preparation method thereof
CN101475487B (en) Recycling use method of nitration acid
CN211123731U (en) Intelligent control reaction system for preparing ethylene glycol based on ethylene hydration method
CN211814210U (en) Micro-interface enhanced reaction system for preparing ethylene glycol based on ethylene hydration method
CN104577122B (en) Lithium iron phosphate solvothermal preparation device
CN105884586B (en) A kind of method and device thereof of methanol gas phase dewatering preparing dimethy ether device combined production of methanol sodium
CN109748805A (en) The method of liquid ammonia process for caustic soda purification production isopropanolamine
CN103553004A (en) Method for continuous preparation of sodium azide
CN202643318U (en) Device for preparing hydrogen fluoride
CN113045451A (en) Method for preparing methoxylamine hydrochloride by adopting microreactor
CN210765081U (en) Production device of urotropine
CN103304442B (en) Process for synthesizing diacetylmonoxime ethyl ether by continuous reactions in microtube
CN102531027A (en) Method for preparing heavy basic copper carbonate
CN104600302A (en) Hot preparation technology of lithium iron phosphate solvent
CN203922752U (en) A kind of device that removes ammonium sulfate and calcium carbonate mixture slurry free ammonia
CN216856337U (en) System for preparing furfural by using hemicellulose or xylose raw material liquid
CN108997127B (en) Production process for synthesizing 1, 3-di- (2-chloro-4-trifluoromethylphenoxy) -4-nitrobenzene
CN211999533U (en) Continuous production system of ammonium adipate
CN210559393U (en) Distillation reaction kettle for purifying reagent-grade nitric acid
CN103387479B (en) Method for water removal and alcohol-water mixed solution separation in alcohol method-based separation purification of arsenic trioxide
CN114345376A (en) Acidic ion buffer solution catalyst, preparation method thereof, and system and method for preparing furfural by using catalyst

Legal Events

Date Code Title Description
C14 Grant of patent or utility model
GR01 Patent grant
C17 Cessation of patent right
CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20130515

Termination date: 20130919