The present disclosure relates to the technical field of biotechnology and polymer synthesis, and discloses a method for producing polylactic acid, the method comprises the following steps: (i) inoculating a lactic acid fermentation strain into a lactic acid fermentation culture medium to perform a fermentation, so as to obtain a fermentation broth containing lactate; (ii) separating the fermentation broth to obtain a lactic acid; (iii) synthesizing a polymer-grade lactide by using the lactic acid as a raw material; (iv) subjecting the polymer-grade lactide to a polymerization reaction in a polymerization reaction device to obtain a polylactic acid. Through the above technical solution, the polylactic acid can be efficiently produced in the present disclosure.

The present invention relates to the technical field of polylactic acid preparation, and discloses polylactic acid polymerization reaction apparatus and system. The polylactic acid polymerization reaction apparatus comprises a polymerization reactor and an agitating assembly arranged in a flow channel of the polymerization reactor, wherein the agitating assembly comprises an electromagnetic winding mechanism and a magnetic induction element, the electromagnetic winding mechanism is arranged along the inner wall of the polymerization reactor around the magnetic induction element, with clearance formed between the electromagnetic winding mechanism and the magnetic induction element, so that the magnetic induction element and the electromagnetic winding mechanism can induce electromagnetic induction, and thereby the magnetic induction element can rotate around its own axis; a threaded groove is formed on the magnetic induction element. The polylactic acid polymerization reaction apparatus provided by the present invention can improve the polymerization effect and thereby improve the product conversion ratio.

In accordance with one embodiment, a processing device includes a heated internal wall and a rotating rod positioned within an interior space formed by the heated internal wall. The rotating rod may be hollow and act as an internal heat exchanger. The processing device also includes a plurality of baffles spaced apart from one another along the rotating rod and extending away from the rotating rod towards the heated internal wall. The plurality of baffles or porous, packed basket that rotates with the rotating rod that also may be configured to provide cooling relative to the heated internal wall. The processing device also includes at least one wiper or roller coupled to an edge of at least one of the plurality of baffles or porous, packed basket, coupled to the rotating rod and that contacts the heated internal wall while rotating together with the rotating rod. In another embodiment, a processing device may be used to adsorb reactive gases into a liquid phase while heat is exchanged.

A continuous acoustic chemical microreactor system is disclosed. The system includes a continuous process vessel (CPV) and an acoustic agitator coupled to the CPV and configured to agitate the CPV along an oscillation axis. The CPV includes a reactant inlet configured to receive one or more reactants into the CPV, an elongated tube coupled at a first end to the reactant inlet and configured to receive the reactants from the reactant inlet, and a product outlet coupled to a second end of the elongated tube and configured to discharge a product of a chemical reaction among the reactants from the CPV. The acoustic agitator is configured to agitate the CPV along the oscillation axis such that the inner surface of the elongated tube accelerates the one or more reactants in alternating upward and downward directions along the oscillation axis.

In at least one embodiment, a reactor includes a reactor body. A first internal heat exchanger and a second internal heat exchanger are within the reactor body. One or more slabs of one or more static inserts are disposed between the first internal heat exchanger and the second internal heat exchanger. A plurality of flow paths is defined between the plurality of flow channels of the first internal heat exchanger and the plurality of flow channels of the second internal heat exchanger. Each static insert is configured to rotate or translate a flow path so that on average, the existing boundary layers formed in the first heat exchanger are moved away from the channel walls by a distance of equal or greater than the thickness of the boundary layers at the exit of the first heat exchanger

A supercritical water oxidation-flame piloted vortex reactor has a hydrothermal flame produced within the interior of the reactor fed by a fuel including a waste water stream, and has a subcritical wash stream, including water below its critical point, that creates an upward helical flow in the material within the reactor. The hydrothermal flame and upward helical flow produce within the reactor a supercritical core region, a subcritical outer region around the core region, and a transcritical intermediate region between them. The upward helical flow serves to transfer precipitated ionic compounds out of the supercritical core region, through the transcritical intermediate region, and into the subcritical outer region where they re-dissolve. A processed flow, including purified water, is removed from an upper portion of the supercritical core region by an aspirator.

A continuous tubular reactor includes a rotary reaction tube having a reactant inlet and a product outlet, and including a ceramic; a heating device disposed outside the rotary reaction tube; and an angle adjuster adjusting an angle of a rotation axis of the rotary reaction tube. The angle of the rotation axis is 75 or less with respect to a horizontal surface.

A fluid distribution system (208) is provided for a reactor vessel (200) defining a reaction chamber (202). The fluid distribution system (208) may include a radial distribution component (224) positionable within the reaction chamber (202) and adjacent a vessel inlet (212) at an end portion of the reactor vessel (200). The radial distribution component (224) may include one or more annular distribution conduits (230) configured to receive a fluid mixture provided to the reactor vessel (200). The fluid distribution system (208) may also include an axial distribution component (226) positionable within the reaction chamber (202) to extend from the radial distribution component (224) along a longitudinal axis of the reactor vessel (200). The axial distribution component (230) may include a plurality of helical conduits (236) fluidly coupled with the one or more annular distribution conduits (230) and configured to receive the fluid mixture from the one or more annular distribution conduits (230) and to disperse the fuel mixture uniformly within the reaction chamber (202).

Method and apparatus for compact and easily maintainable waste reformation. Some embodiments include a rotary oven reformer adapted and configured to provide synthesis gas from organic waste. Some embodiments include a rotary oven with simplified operation both as to reformation of the waste, usage of the synthesized gas and other products, and easy removal of the finished waste products, preferably in a unit of compact size for use in austere settings. Yet other embodiments include Fischer-Tropsch reactors of synthesized gas. Some of these reactors include heat exchanging assemblies that provide self-cleaning effects, efficient utilization of waste heat, and ease of cleaning.

A continuous flow reactor includes a shell, wherein the shell is provided with a shell pass inlet and a shell pass outlet which are communicated with an inner cavity of the shell, tube plates and communication devices are connected to upper and lower ends of the shell, a reaction tube bank is arranged in the shell and includes a plurality of reaction tubes, upper and lower ends of each reaction tube are fixedly connected to the tube plates in a penetrating manner, and all the reaction tubes are sequentially communicated in series through the communication devices.