CN203916121U - DMAC reclaims physical property index optimization system - Google Patents
DMAC reclaims physical property index optimization system Download PDFInfo
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- CN203916121U CN203916121U CN201420333284.1U CN201420333284U CN203916121U CN 203916121 U CN203916121 U CN 203916121U CN 201420333284 U CN201420333284 U CN 201420333284U CN 203916121 U CN203916121 U CN 203916121U
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Abstract
The utility model relates to a kind of DMAC and reclaims physical property index optimization system, belongs to spandex production technical field.Comprise dehydrating tower, thick flux bath, treating column, distillation still feed trough and recovery tower, dehydrating tower connects feed pipe, and the bottom of dehydrating tower is communicated to treating column middle part by thick flux bath, and treating column bottom is communicated with recovery tower bottom by distillation still feed trough; Described dehydrating tower middle part is connected with preheater, and top is connected with condenser one and deep freezer one; Treating column top is connected with condenser two and deep freezer two; Recovery tower top arranges condenser three, and condenser three is provided with condensate receiver three, and condenser three tops arrange vavuum pump three.Adopt the utility model to carry out the recovery of DMAC in spandex production process, not only guarantee that DMAC distillation system normally moves, and output and the physical index of recovery gained DMAC are all greatly enhanced.
Description
Technical field
The utility model relates to a kind of DMAC (N, N dimethylacetylamide) and reclaims physical property index optimization system, by the technological transformation to DMAC distillation system dehydrating tower and rectifying column, realizes and optimizes the optimization of DMAC physical index, belongs to spandex production technical field.
Background technology
In chemical process, usually need raw material, intermediate product or crude product to carry out separation, to obtain chemical products or the intermediate products that meet technological requirement.On chemical industry, common separation process comprises distillation, absorption, extraction, dry and crystallization etc., and wherein distillation is the typical unit operation of separating liquid mixture, is most widely used.Polyurethane fiber dry spinning technique needs a large amount of DMAC of use to recycle as solvent, and in solvent dry spinning process, PTMG and MDI carry out prepolymerization under DMAC solvent exists, and by amine chain extension, form macromolecule polyurethane polymer.DMAC solvent gasifies by high temperature path, through SM system cools, forms liquids recovery to USW-STK.The DMAC liquid that spinning process USW-RTK reclaims is dewatered, is got back to polymerization recycling after rectifying by refining system, in this process, need to remove moisture, metal ion, acid minute and high-boiling components etc., but traditional plate column or old-fashioned packed tower cannot reach higher purification requirement, and energy consumption is high.
Based on the problems referred to above, the application's case produces thus.
Utility model content
There is the defects such as separative efficiency is low, energy consumption is high, complex operation in existing distillation system filler, for overcoming the above-mentioned shortcoming of distillation system, the utility model provides the DMAC that a kind of separative efficiency is high, easy to operate, energy consumption is low to reclaim materialization index optimization system.
For achieving the above object, the technical scheme that the utility model is taked is as follows:
DMAC reclaims physical property index optimization system, comprise dehydrating tower, thick flux bath, treating column, distillation still feed trough and recovery tower, dehydrating tower connects feed pipe, and the bottom of dehydrating tower is communicated to treating column middle part by thick flux bath, and treating column bottom is communicated with recovery tower bottom by distillation still feed trough; Described dehydrating tower middle part is connected with preheater, top is connected with condenser one and deep freezer one, condenser one is provided with condensate receiver one, condensate receiver one is communicated with dehydrating tower by return duct one, deep freezer one bottom communicates with condensate receiver one, and deep freezer one top arranges vavuum pump one; Treating column top is connected with condenser two and deep freezer two, condenser two is provided with condensate receiver two, condensate receiver two is communicated with treating column and head tank one respectively by return duct two and recovery tube one, deep freezer two bottoms communicate with condensate receiver two, and deep freezer two tops arrange vavuum pump two; Recovery tower top arranges condenser three, and condenser three is provided with condensate receiver three, and condensate receiver three is communicated with recovery tower and head tank two respectively by return duct three and recovery tube two, and condenser three tops arrange vavuum pump three; Vavuum pump one, vavuum pump two, vavuum pump three are connected with water spray column by pipeline respectively, and water spray column absorbs the DMAC aqueous solution obtaining and through pipeline, sends into preheater, and sends dehydrating tower back to through preheater.
Further, as preferably:
In described dehydrating tower, feed pipe absolute altitude 17500mm, return duct one absolute altitude is 28490mm, the interior slotted disk distributor one that arranges of catch box one at feed pipe place, the slotted disk one of slotted disk distributor one is 411mm with the vertical range of feed tube, slotted disk distributor one perforate number is 2000, and the diameter in hole is 4mm; The dehydrating tower middle part corresponding with return duct one arranges groove type distributor one, and the perforate number of groove type distributor one is 2300, and the diameter in hole is 3mm, and its elevation of bottom is 28577mm, and vertical range is 580mm; Two sections of packing section between groove type distributor one and slotted disk distributor one one minute, one section of be 1m CY filler and 1.4mBX filler combination, BX filler that another section is 3m; (spotting out rate 82%, R=5), stripping section comprises two sections of BX fillers that are highly 2.5m, between two sections of BX fillers, integral type distributor is set in the stripping section at dehydrating tower top, to adopt CJ-350Y.
In described treating column, return duct two absolute altitudes are 30210mm, in the treating column of thick flux bath and treating column connectivity part, catch box two are set, and catch box two is set to slotted disk distributor two, slotted disk distributor two arranges side and extracts mouth out in absolute altitude 23505mm place, slotted disk distributor bottom is provided with BX filler; The treating column middle part corresponding with return duct two arranges groove type distributor two, and the perforate number of groove type distributor two is 2800, and the diameter in hole is 4mm, and its elevation of bottom is 28961mm, and vertical range is 140mm; The BX filler that packing section two between groove type distributor two and slotted disk distributor two is 3m.
The install pipeline that described thick flux bath is communicated with treating column has pipeline support.
The specification of described feed pipe is DN50; Return duct one specification is DN50, and return duct two specifications are DN65.
While adopting the utility model to carry out DMAC recovery, the thick flux bath of direct warp that a solution part of sending into through feed pipe is dewatered up to standard through dehydrating tower is sent into treating column, after treating column is refining, through distillation still feed trough, send into recovery tower again, and it is stand-by to send into head tank two after condenser three condensation process, or squeeze into water spray column by vavuum pump three, another part dehydration solution not up to standard enters for one time in dehydrating tower to continue to dewater through reboiler, and after condenser one condensation, return to dehydrating tower and repeat dehydration, finally by deep freezer one, vavuum pump one, squeezed into vavuum pump two places at water spray column or remittance treating column place, after treating column is refining, solution not up to standard enters in treating column for two times through reboiler, after treating column evaporator overhead condenser two condensation process, a part is returned treating column and is repeated to refine, complete refining solution and send into head tank one or DMAC storage tank by treating column middle part, another part is sent into after deep freezer two processing after condenser two is processed, through condensate receiver two, send into head tank one or pass back into treating column, or through the vavuum pump two at deep freezer two tops, squeeze into vavuum pump three places at water spray column or remittance recovery tower place, vavuum pump one, vavuum pump two imports water spray column place in the lump with the solution of vavuum pump three, through water spray column, absorb and form after the DMAC aqueous solution, send into after preheater preheating, by dehydrating tower middle part, sent into, the dehydration circulating, refine and reclaim, until up to standard.
Employing the utlity model has following beneficial effect:
1. the DMAC that the utility model adopts reclaims in physical property index optimization system, dehydrating tower, treating column and recovery tower are provided with backflow, condensation and subzero treatment, the DMAC aqueous solution has only reached the standard of setting and just can be admitted in DMAC storage tank or is standby in head tank, based on backflow, condensation, the special circuit design of deep cooling, guaranteed under DMAC distillation system normal operating condition, make the DMAC moisture reclaiming, metal ion, acid minute and high-boiling components the physical index such as remove and are all better than conventional distillation system recovering effect, its moisture content≤50ppm, acid number≤30ppm, basicity (in dimethylamine)≤5ppm, DMAC output (in finished product) is higher than 35 tons/day.
2. the utility model is optimized design to the absolute altitude at the parts such as the filler of dehydrating tower and treating column inside, distributor, feeding line, catch box and core position and distance, not only can prevent gas, liquid is short out road, guarantee dehydration, refine fast, efficiently carry out, the output of DMAC is improved greatly, corresponding cost recovery also reduces greatly, and Overall Reconstruction and simplicity of design are easy to operate, can conveniently on existing equipment, be optimized improvement, and improving cost is limited, utilization rate of equipment and installations improves greatly.
3. arranging of vavuum pump one, vavuum pump two and vavuum pump three is mainly that the solution of its position is returned in water spray column, and therefore, the material that can adopt identical vacuum can meet three places shifts demand, and power consumption is controlled.
4. to arrange be to combine the unique design that gravity in perforate situation and solution reflux course and energy consumption are carried out in the position of return duct, feed pipe and each distributor, this unique design can still can be carried out normally the refining of DMAC and be reclaimed under lower reflux ratio and circulating water cooling system, therefore, power station, without HW7 degree water system, is saved operation energy consumption and investment greatly.
Adopt the utility model to carry out the recovery of DMAC in spandex production process, not only guaranteed that material shifts and refining demand, guarantee that DMAC distillation system normally moves, and output and the physical index of recovery gained DMAC are all greatly enhanced.
Accompanying drawing explanation
Fig. 1 is the structural representation of the utility model recovery system;
Fig. 2 is the structural representation of the utility model dehydrating tower;
Fig. 3 is the structural representation of the utility model treating column.
Number in the figure: 1. dehydrating tower; 1a. condenser one; 1b. deep freezer one; 1c. condensate receiver one; 1d. return duct one; 1e. vavuum pump one; 11. refluxing openings one; 12. charging apertures one; 13. reboiler one interfaces; 14. steam vents one; 15. dehydration overhead gas outlets; 16. discharging openings one; 17. manholes one; 18. slotted disk distributors one; 19. groove type distributors one; 2. thick flux bath; 3. treating column; 3a. condenser two; 3b. deep freezer two; 3c. condensate receiver two; 3d. return duct two; 3e. vavuum pump two; 3f. head tank one; 3g.DMAC storage tank; 3h. recovery tube one; 31. charging apertures two; 32. refining overhead gas outlets; 33. refluxing openings two; 34. reboiler two interfaces; 35. discharging openings two; 36. sides are extracted mouth out; 37. manholes two; 4. distillation still feed trough; 5. recovery tower; 5a. condenser three; 5b. vavuum pump three; 5c. condensate receiver three; 5d. return duct three; 5e. head tank two; 5f. recovery tube two; 6. water spray column; 7. preheater; 8. feed pipe; 9a. reboiler one; 9b. reboiler two.
The specific embodiment
The present embodiment DMAC reclaims physical property index optimization system, in conjunction with Fig. 1, comprise dehydrating tower 1, thick flux bath 2, treating column 3, distillation still feed trough 4 and recovery tower 5, dehydrating tower 1 connects feed pipe 8, dehydrating tower 1 bottom is communicated to treating column 3 middle parts by thick flux bath 2, and treating column 3 bottoms are communicated with recovery tower 5 bottoms by distillation still feed trough 4; Dehydrating tower 1 middle part is connected with preheater 7, top is connected with condenser one 1a and deep freezer one 1b, condenser one 1b is provided with condensate receiver one 1c, condensate receiver one 1c is communicated with dehydrating tower 1 by return duct one 1d, deep freezer one 1b bottom communicates with condensate receiver one 1c, and deep freezer one 1b top arranges vavuum pump one 1e; Treating column 3 tops are connected with condenser two 3a and deep freezer two 3b, condenser two 3a are provided with condensate receiver two 3c, condensate receiver two 3c are communicated with treating column 3 by return duct two 3d, condensate receiver two 3c are communicated with head tank one 3f by recovery tube one 3h, deep freezer two 3b bottoms communicate with condensate receiver two 3c, and deep freezer two 3b tops arrange vavuum pump two 3e; Recovery tower 5 tops arrange condenser three 5a, condenser three 5a are provided with condensate receiver three 5c, condensate receiver three 5c are communicated with recovery tower 5 by return duct three 5d, and condensate receiver three 5c are communicated with head tank two 5e by recovery tube two 5f, and condenser three 5a tops arrange vavuum pump three 5b; Vavuum pump one 1e, vavuum pump two 3e, vavuum pump three 5b are connected with water spray column 6 by pipeline respectively, and water spray column 6 absorbs the DMAC aqueous solution obtaining and through pipeline, sends into preheater 7, and sends dehydrating tower 1 back to through preheater 7.Wherein:
In conjunction with Fig. 2, in dehydrating tower 1, feed pipe 8 is connected to charging aperture 12 places, condenser one 1a is connected to dehydration overhead gas and exports 15 places, and thick flux bath 2 is connected to discharging opening one 16 places by pipeline, and feed pipe 8 is connected to charging aperture one 11 places, feed pipe 8 changes DN50 into, absolute altitude 17500mm; Return duct one 1d is connected to refluxing opening one 11 places, changes return duct one 1d, by original DN25, changes DN50 into, and return duct one 1d absolute altitude is 28490mm; Determine the percent opening at feed pipe 8 places, by the interior slotted disk distributor 1 that arranges of the catch box one at feed pipe 8 places, the slotted disk one of slotted disk distributor 1 is 411mm with the vertical range of feed tube, and slotted disk distributor one 18 perforate numbers are 2000, and the diameter in hole is 4mm; Determine after the percent opening at return duct one 1d place, dehydrating tower 1 middle part corresponding with return duct one 1d is set to groove type distributor 1, and trim ring reuses, the perforate number of groove type distributor 1 is 2300, the diameter in hole is 3mm, and its elevation of bottom is 28577mm, and vertical range is 580mm; Two sections of packing section between groove type distributor 1 and slotted disk distributor 1 one minute, one section of be 1m CY filler and 1.4mBX filler combination, BX filler that another section is 3m; Filler employing CJ-350Y in the stripping section at dehydrating tower 1 top (spotting out rate 82%, R=5), stripping section comprises two sections of BX fillers that are highly 2.5m, between two sections of BX fillers, integral type distributor is set; Former tower M2, M3 two manholes 17 add steel plate, polish smooth, and prevent gas, liquid short circuit.
In conjunction with Fig. 3, in treating column 3, thick flux bath 2 is connected to charging aperture 2 31 places by pipeline, condenser two 3a are connected to refining overhead gas and export 32 places, reboiler 2 92 is connected to reboiler two interface 34 places, and distillation still feed trough 4 is connected to discharging opening 2 35 places, and return duct two 3d are connected to refluxing opening 2 33 places, by original DN25, change return duct two 3d into DN65, return duct two 3d absolute altitudes are 30210mm; Determine the percent opening in the treating column 3 of thick flux bath 2 and treating column 3 connectivity parts, catch box two is set to slotted disk distributor two and (does squarely, other spaces are for cloth liquid), slotted disk distributor two arranges side and extracts mouth 36 out in absolute altitude 23505mm place, and slotted disk distributor bottom is provided with BX filler; Treating column 3 middle parts corresponding with return duct two 3d arrange groove type distributor two, and the perforate number of groove type distributor two is 2800, and the diameter in hole is 4mm, and its elevation of bottom is 28961m, and vertical range is 140mm; The BX filler that packing section two between groove type distributor two and slotted disk distributor two is 3m.
Process conditions and the concrete ginseng of material balance relationship that above-mentioned DMAC reclaims physical property index optimization system are shown in Table 1.When carrying out DMAC recovery, a solution part of sending into through feed pipe 8 is sent into treating column 3 through the dehydrating tower 1 dehydration thick flux bath 2 of direct warp up to standard, after treating column 3 is refining, through distillation still feed trough 4, send into recovery tower 5 again, and it is stand-by to send into head tank two 5e after condenser three 5a condensation process, or squeeze into water spray column 6 by vavuum pump three 5b, another part dehydration solution not up to standard returns in dehydrating tower 1 and continues to dewater through reboiler one 9a, and after condenser one 1a condensation, return to dehydrating tower 1 and repeat dehydration, finally by deep freezer one 1b, vavuum pump one 1e, squeezed into the vavuum pump two 3e places at water spray column 6 or remittance treating column 3 places, after treating column 3 is refining, solution not up to standard returns in treating column 3 through reboiler two 9b, after treating column 3 evaporator overhead condenser two 3a condensation process, a part is returned treating column 3 and is repeated to refine, complete refining solution and send into head tank one 3f or DMAC storage tank 3g by treating column 3 middle parts, another part is sent into after deep freezer two 3b processing after condenser two 3a process, through condensate receiver two 3c, send into head tank one 3f or pass back into treating column 3 through return duct two 3d, or vavuum pump two 3e through deep freezer two 3b tops squeeze into water spray column 6 or import the vavuum pump three 5b places at recovery tower 5 places, vavuum pump one 1e, the solution of vavuum pump two 3e and vavuum pump three 5b imports water spray column 6 places in the lump, through water spray column 6, absorb and form after the DMAC aqueous solution, send into after preheater 7 preheatings, by dehydrating tower 1 middle part, sent into, the dehydration circulating, refine and reclaim, until up to standard.
Table 1 material balance table
According to scheme that the present embodiment provides, carry out DMAC recovery, its recovering effect can be joined and is shown in Table 2.
The physical index table of comparisons that in table 2 the present embodiment, DMAC reclaims
As can be seen from Table 2, cleaning after DAMC distillation system reincarnate, pressure test leak-detecting, driving operation, DMAC index reaches designing requirement completely.
Economic operation analysis:
1. vacuum system TW-1, TW-2 shares a set of vavuum pump, adopts identical vacuum, saves electric power.
2. the refining cost of ton DMAC finished product can reach 200 yuan (approximately 405 yuan of the refining ton of existing system DMAC product costs), wherein ton DMAC is refining need to consume approximately 0.529 ton of steam (0.4MPA), the about 35.5KW of power consumption and 325863 kilocalorie refrigeration dutys.
3. this technology reforming scheme is simple, only the filler of two towers and tower internals need design to changing concludes the business and whole refining system is redesigned and debugged can reach designing requirement.
4. technological transformation reaches a day ability of refining 40 tons of DMAC after completing.
5. for energy-conservation, this transformation will adopt lower reflux ratio and circulating water cooling system, and power station, without HW7 degree water system, will be saved operation energy consumption and investment so greatly.All heat exchangers, heater, overhead condenser, reboilers etc. all pass through design and dry run, and heat exchange area all can meet Technical Revamping Design requirement.
Claims (5)
1.DMAC reclaims physical property index optimization system, it is characterized in that: comprise dehydrating tower, thick flux bath, treating column, distillation still feed trough and recovery tower, dehydrating tower connects feed pipe, dehydrating tower bottom is communicated to treating column middle part by thick flux bath, and treating column bottom is communicated with recovery tower bottom by distillation still feed trough; Described dehydrating tower middle part is connected with preheater, top is connected with condenser one and deep freezer one, condenser one is provided with condensate receiver one, condensate receiver one is communicated with dehydrating tower by return duct one, deep freezer one bottom communicates with condensate receiver one, and deep freezer one top arranges vavuum pump one; Treating column top is connected with condenser two and deep freezer two, condenser two is provided with condensate receiver two, condensate receiver two is communicated with treating column and head tank one respectively by return duct two and recovery tube one, deep freezer two bottoms communicate with condensate receiver two, and deep freezer two tops arrange vavuum pump two; Recovery tower top arranges condenser three, and condenser three is provided with condensate receiver three, and condensate receiver three is communicated with recovery tower and head tank two respectively by return duct three and recovery tube two, and condenser three tops arrange vavuum pump three; Vavuum pump one, vavuum pump two, vavuum pump three are connected with water spray column by pipeline respectively, and water spray column absorbs the DMAC aqueous solution obtaining and through pipeline, sends into preheater, and sends dehydrating tower back to through preheater.
2. DMAC as claimed in claim 1 reclaims physical property index optimization system, it is characterized in that: in described dehydrating tower, feed pipe absolute altitude 17500mm, return duct one absolute altitude is 28490mm, the interior slotted disk distributor one that arranges of catch box one at feed pipe place, the slotted disk one of slotted disk distributor one is 411mm with the vertical range of feed tube, and slotted disk distributor one perforate number is 2000, and the diameter in hole is 4mm; The dehydrating tower middle part corresponding with return duct one arranges groove type distributor one, and the perforate number of groove type distributor one is 2300, and the diameter in hole is 3mm, and its elevation of bottom is 28577mm, and vertical range is 580mm; Two sections of packing section between groove type distributor one and slotted disk distributor one one minute, one section is CY filler and BX filler combination, another section is BX filler; The stripping section at dehydrating tower top comprises two sections of highly identical BX fillers, between two sections of BX fillers, integral type distributor is set.
3. DMAC as claimed in claim 1 reclaims physical property index optimization system, it is characterized in that: in described treating column, return duct two absolute altitudes are 30210mm, in the treating column of thick flux bath and treating column connectivity part, catch box two is set, catch box two is set to slotted disk distributor two, slotted disk distributor two arranges side and extracts mouth out in absolute altitude 23505mm place, slotted disk distributor bottom is provided with BX filler; The treating column middle part corresponding with return duct two arranges groove type distributor two, and the perforate number of groove type distributor two is 2800, and the diameter in hole is 4mm, and its elevation of bottom is 28961mm, and vertical range is 140mm; Packing section two between groove type distributor two and slotted disk distributor two is BX filler.
4. DMAC as claimed in claim 1 reclaims physical property index optimization system, it is characterized in that: the install pipeline that described thick flux bath is communicated with treating column has pipeline support.
5. DMAC as claimed in claim 1 reclaims physical property index optimization system, it is characterized in that: the specification of described feed pipe is DN50; Return duct one specification is DN50, and return duct two specifications are DN65.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420333284.1U CN203916121U (en) | 2014-06-20 | 2014-06-20 | DMAC reclaims physical property index optimization system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420333284.1U CN203916121U (en) | 2014-06-20 | 2014-06-20 | DMAC reclaims physical property index optimization system |
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| Publication Number | Publication Date |
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| CN203916121U true CN203916121U (en) | 2014-11-05 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201420333284.1U Withdrawn - After Issue CN203916121U (en) | 2014-06-20 | 2014-06-20 | DMAC reclaims physical property index optimization system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104043260A (en) * | 2014-06-20 | 2014-09-17 | 浙江开普特氨纶有限公司 | Physical index optimizing system for recycling DMAC (dimethylacetamide) |
| CN104478752A (en) * | 2014-11-25 | 2015-04-01 | 江阴中绿化纤工艺技术有限公司 | DMAC refining system for spandex spinning production process |
| CN109111005A (en) * | 2018-09-19 | 2019-01-01 | 四川久润环保科技有限公司 | A kind of method and system of the high purity DMAC from industrial wastewater |
-
2014
- 2014-06-20 CN CN201420333284.1U patent/CN203916121U/en not_active Withdrawn - After Issue
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104043260A (en) * | 2014-06-20 | 2014-09-17 | 浙江开普特氨纶有限公司 | Physical index optimizing system for recycling DMAC (dimethylacetamide) |
| CN104043260B (en) * | 2014-06-20 | 2016-07-06 | 浙江开普特氨纶有限公司 | DMAC reclaims physical property index optimization system |
| CN104478752A (en) * | 2014-11-25 | 2015-04-01 | 江阴中绿化纤工艺技术有限公司 | DMAC refining system for spandex spinning production process |
| CN104478752B (en) * | 2014-11-25 | 2016-03-09 | 江阴中绿化纤工艺技术有限公司 | A kind of spandex fiber production process DMAC refining system |
| CN109111005A (en) * | 2018-09-19 | 2019-01-01 | 四川久润环保科技有限公司 | A kind of method and system of the high purity DMAC from industrial wastewater |
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| AV01 | Patent right actively abandoned |
Granted publication date: 20141105 Effective date of abandoning: 20160706 |
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| C25 | Abandonment of patent right or utility model to avoid double patenting |